A process and apparatus for oilfield produced fluid dehydration and water treatment

Abstract

The application provides a kind of oilfield produced liquid dehydration and water treatment equipment, comprising: first chamber and second chamber, the first chamber includes density difference separation chamber, dielectric difference separation chamber and buffer chamber;The second chamber includes enhanced oil removal chamber and removes suspended solid chamber;The first chamber and the second chamber constitute a pot structure;The length-diameter ratio of the pot structure is 3 to 6.The application is based on the concept of crude oil dehydration and water treatment overall consideration and efficient oil-water separation mechanism, proposes a multifunctional integration, which can complete efficient crude oil dehydration, and can also remove oil in water Process system and equipment, solve the problems of large occupied area, long process, many equipment, large VOCs emission, complex operation and other problems caused by the separation construction of previous oilfield produced water dehydration section and water treatment section, compared with more than 10 devices of traditional process, the produced liquid treatment process greatly reduces the number of running equipment.

Description

Technical Field

[0001] This article relates to, but is not limited to, the field of oil and gas field produced fluid dehydration and water treatment, and particularly to, but is not limited to, a process and equipment for oil field produced fluid dehydration and water treatment system. Background Technology

[0002] With the increasing deterioration of oilfield resources, most new oilfield production capacity expansions or densification efforts are now focused on expanding existing facilities. The design scale of new dehydration stations is significantly reduced compared to the past. In some oilfields, due to the compatibility of produced water, stratified extraction and treatment are required, further exacerbating this situation. Some newly built dehydration stations have a treatment capacity of only tens of thousands of cubic meters per year. Existing crude oil dehydration systems are designed for separating oil particles with a diameter greater than 200μm and an oil content in the effluent of less than 1000mg / L. The high oil content in the water increases the difficulty of water system treatment. To meet injection water quality requirements, water treatment systems also employ long main processes such as multi-stage sedimentation and filtration. Secondary processes include oily waste tanks, wastewater recovery ponds, and sludge thickening facilities. Traditional dehydration and water treatment main processes include... Figure 1 As shown:

[0003] If the traditional dewatering process and construction model are continued in newly built small and medium flow stations, although the processing flow is not large, it will inevitably bring problems such as long process, large number of equipment, complex supporting facilities such as on-site pipes, valves and pumps, large area, complicated operation, large workload of manual maintenance and inspection, and large VOCs emissions from many facilities and storage tanks such as oil-water buffer tanks, natural settling tanks, coagulation settling tanks and buffer tanks.

[0004] Existing dehydration and water treatment processes and construction models are no longer suitable for the efficient and low-cost development needs of oilfield produced fluids. They suffer from problems such as long dehydration and water treatment systems, numerous devices, high VOC emissions, and complex operation. The connection between dehydration and water treatment equipment requires extensive pipelines, pumps, valves, etc., posing environmental and safety risks such as secondary pollution and leaks. Revolutionary measures are urgently needed to adapt to the changing development landscape.

[0005] In view of the contradictions and problems existing in the current dehydration and water treatment processes and construction models, it is not advisable to continue to adopt the original construction model. It is necessary to break down professional boundaries based on new concepts, to consider the crude oil dehydration system and water treatment system as a whole, and to propose new processes and equipment to simplify the crude oil dehydration and water treatment processes, so as to achieve the goals of simplifying the process, reducing costs and improving efficiency. Summary of the Invention

[0006] The following is an overview of the subject matter described in detail herein. This overview is not intended to limit the scope of the claims.

[0007] This application provides an oilfield produced fluid dehydration and water treatment device, including:

[0008] A first chamber and a second chamber, wherein the first chamber includes a density difference separation chamber, a dielectric difference separation chamber, and a buffer chamber; and the second chamber includes an enhanced degreasing chamber and a suspended solids removal chamber.

[0009] The first chamber and the second chamber form a can-shaped structure; the aspect ratio of the can-shaped structure is 3 to 6.

[0010] In one embodiment provided in this application, the density difference separation chamber is configured to perform oil-water separation and / or solid-liquid separation through the density difference of the oilfield produced fluid;

[0011] The dielectric difference separation chamber is configured to perform oil-water separation and / or solid-liquid separation via dielectric difference.

[0012] The enhanced oil removal chamber is configured to perform oil-water separation and / or solid-liquid separation through one or more of micro-vortex coalescence and density difference.

[0013] The suspended solids removal chamber is configured to perform oil-water separation and / or solid-liquid separation by any one or more of flocculation reaction and / or density difference.

[0014] In one embodiment provided in this application, the density difference separation chamber is provided with a liquid inlet device, a three-phase separation device, a first liquid outlet and a second liquid outlet.

[0015] In one embodiment provided in this application, the liquid inlet device is configured to separate the gas phase and the liquid phase by cyclone separation, including a cyclone liquid inlet device, a rake-type liquid distribution pipe and a rectifier plate;

[0016] The three-phase separation device includes a coalescing inclined plate assembly;

[0017] The dielectric differential separation chamber is provided with an electrode plate assembly, a first gas outlet, and a third liquid outlet.

[0018] In one embodiment provided in this application, the enhanced oil removal chamber is provided with at least one micro-vortex coalescing chamber and at least one inclined tube oil removal chamber.

[0019] In one embodiment provided in this application, the micro vortex coalescing chamber and the inclined tube oil removal chamber are configured such that liquid flows sequentially through the micro vortex coalescing chamber and the inclined tube oil removal chamber;

[0020] The micro vortex coalescing chamber is equipped with a first liquid inlet and a micro vortex coalescing device.

[0021] There are two or more micro vortex coalescing chambers, and the liquid flowing out of the first inlet passes through all the micro vortex coalescing chambers in sequence.

[0022] The inclined tube oil removal chamber is provided with a downward-flow inclined tube group and a fourth liquid outlet.

[0023] In an embodiment provided by the present application, the second liquid outlet and the third liquid outlet are in communication with the first liquid inlet.

[0024] In an embodiment provided by the present application, the suspended solid removal chamber is provided with at least a contact reaction chamber and an inclined plate suspended solids removal chamber.

[0025] In an embodiment provided by the present application, the contact reaction chamber and the inclined plate suspended solids removal chamber are configured such that liquid flows through the contact reaction chamber and the inclined plate suspended solids removal chamber in sequence;

[0026] The contact reaction chamber is provided with at least a second liquid inlet and a contact reaction promoting device;

[0027] There are two or more contact reaction chambers, and the liquid flowing out from the second liquid inlet passes through all the contact reaction chambers in sequence;

[0028] The inclined plate suspended solids removal chamber is provided with at least a 丰-shaped inclined plate group and an equipment water outlet.

[0029] In an embodiment provided by the present application, the fourth liquid outlet is in communication with the second liquid inlet;

[0030] Alternatively, the fourth liquid outlet is in communication with the second liquid inlet; a chemical feeding pipe is further provided on the pipeline between the fourth liquid inlet and the second liquid inlet.

[0031] In an embodiment provided by the present application, the density difference separation chamber in the first chamber is adjacent to the dielectric difference separation chamber in the second chamber;

[0032] A buffer weir plate is provided between the density difference separation chamber and the dielectric difference separation chamber;

[0033] The buffer weir plate is configured such that when the liquid level in the density difference separation chamber is higher than the top of the buffer weir plate, the liquid in the density difference separation chamber flows over the buffer weir plate and enters the dielectric difference separation chamber.

[0034] In an embodiment provided by the present application, the 丰-shaped inclined plate comprises a fin and a support plate supporting the fin;

[0035] The fin is configured to block the fluid in the 丰-shaped inclined plate group from flowing along the length direction of the support plate.

[0036] In an embodiment provided by the present application, the 丰-shaped inclined plate is configured such that the flowing direction of the fluid passing through the 丰-shaped inclined plate forms an angle of 45° to 80° with the horizontal plane.

[0037] In one embodiment of this application, the ratio of the spacing between adjacent winglets to the height of the winglet (the height of the winglet is the length of the winglet perpendicular to the length direction of the support plate) is (10 to 60):(10 to 60); in one embodiment of this application, the height of the winglet can be 10mm to 60mm.

[0038] In one embodiment provided in this application, the ratio of the height of the winglet to the distance between two adjacent support plates is (10 to 60):(40 to 150).

[0039] In one embodiment provided in this application, the micro-vortex coalescing chamber includes a micro-vortex coalescing device; the micro-vortex coalescing device is a micro-vortex coalescing sphere filled with coalescing packing material, and the micro-vortex coalescing device has a hollow structure, comprising:

[0040] A porous shell; the porous shell is provided with guide holes that connect the inside and outside of the micro vortex coalescing device;

[0041] The coalescing packing is disposed within the hollow structure.

[0042] The longest diameter of the flow guide hole is smaller than the shortest diameter of the coalescing packing.

[0043] In one embodiment provided in this application, the flow guide hole occupies 30% to 80% of the area of ​​the porous housing.

[0044] In one embodiment of this application, the micro vortex coalescing device is a sphere; in one embodiment of this application, the ratio of the outer diameter of the micro vortex coalescing device to the thickness of the porous shell is (100 to 300):(1 to 6); in one embodiment of this application, the ratio of the outer diameter of the micro vortex coalescing device to the diameter-length ratio of the guide hole is (100 to 300):(15 to 40).

[0045] In one embodiment provided in this application, a plurality of coalescing packings in a micro vortex coalescing device have space for rotational movement within a porous shell.

[0046] In one embodiment provided in this application, the porous shell material can be selected from any one or more plastic materials such as ABS, modified ABS, polypropylene, modified polypropylene, and polyethylene.

[0047] In one embodiment provided in this application, the material of the coalescing filler can be selected from any one or more plastic materials such as ABS, modified ABS, polypropylene, modified polypropylene, and polyethylene.

[0048] In one embodiment provided in this application, the length ratio of the outer diameter of the micro vortex coalescing device to the outer diameter of the coalescing packing is 1:(0.125 to 0.5).

[0049] In one embodiment provided in this application, the outer diameter of the micro vortex coalescing device can be from 100 mm to 300 mm.

[0050] In one embodiment provided in this application, the outer diameter of the coalescing packing can be from 25 mm to 75 mm. In another embodiment provided in this application, the outer diameter of the coalescing packing is larger than the diameter of the flow guide hole.

[0051] In one embodiment provided in this application, the coalescing packing is selected from any one or more of Pall ring packing, stepped ring packing, rectangular saddle ring packing, multifaceted hollow sphere packing, hollow sphere packing, porous sphere packing, Raschig ring packing, heterosaddle ring packing, and gear ring packing.

[0052] In one embodiment provided in this application, the average material density of the micro-vortex coalescing device is 0.90 × 10⁻⁶. 3 kg / m 3 Up to 1.1×10 3 kg / m 3 .

[0053] In one embodiment provided in this application, an oil weir plate is provided between the buffer cavity and the dielectric differential separation cavity;

[0054] The oil outlet weir plate is configured such that liquid in the dielectric differential separation chamber that is above the oil outlet weir plate overflows the oil outlet weir plate and enters the buffer chamber.

[0055] In one embodiment provided in this application, the dielectric differential separation chamber is connected to the enhanced degreasing chamber via a pipeline, and the enhanced degreasing chamber is connected to the suspended solids removal chamber.

[0056] In one embodiment provided in this application, the fluid movement direction in the micro-vortex coalescing chamber is perpendicular to the length direction of the can-shaped structure;

[0057] Alternatively, the direction of fluid movement in the contact reaction chamber is perpendicular to the length direction of the tank-like structure;

[0058] Alternatively, the direction of fluid movement in the micro-vortex coalescence chamber and the contact reaction chamber is perpendicular to the length direction of the canister structure.

[0059] On another front, this application provides a method for dehydrating and treating oilfield produced fluids, using the aforementioned oilfield produced fluid dehydration and water treatment equipment, comprising:

[0060] The residence time in the density difference separation chamber is 15 min to 90 min, preferably 30 min to 45 min;

[0061] The residence time of the dielectric differential separation cavity is 10 min to 90 min, preferably 30 min to 45 min;

[0062] The residence time in the enhanced degreasing chamber is 20 min to 90 min, preferably 35 min to 40 min;

[0063] The residence time in the cavity for removing suspended solids is 15 min to 90 min, preferably 30 min to 40 min;

[0064] The residence time in the buffer chamber is 10 min to 60 min, preferably 10 min to 20 min;

[0065] In one embodiment provided in this application, the oilfield produced fluid dehydration and water treatment equipment outputs purified oil with a water content of less than 0.5%, and the gas separated from the produced fluid contains produced water with an oil content and suspended solids content of less than 50 mg / L.

[0066] In one embodiment provided in this application, the above-mentioned oilfield produced fluid dehydration and water treatment equipment, as well as water treatment filtration system, clean water tank, recycled water tank, sludge tank and sludge oil tank are used.

[0067] After the oilfield produced fluid is treated with a demulsifier, it enters the oilfield produced fluid dehydration and water treatment equipment to separate gas, purified oil, produced water and sludge.

[0068] The gas is transported to the natural gas processing system, the purified oil is directly transported out from the buffer chamber through the pipeline, and the produced water is stored in the clean water tank after being filtered by a single or multi-stage filter and then transported out. The backwash water obtained by the device used for backwashing the produced water enters the recovery water tank and then flows back to the enhanced oil removal chamber of the oilfield produced fluid dehydration and water treatment equipment.

[0069] The oily waste collected in the enhanced oil removal chamber is stored in the oily waste tank and then returned to the oilfield produced fluid inlet of the oilfield produced fluid dehydration and water treatment equipment. The sludge separated by the oilfield produced fluid dehydration and water treatment equipment is stored in the sludge tank and transported off-site for treatment.

[0070] This application, based on the concept of integrated crude oil dehydration and water treatment and the efficient oil-water separation mechanism, proposes a multi-functional integrated process system and equipment that can efficiently dehydrate crude oil and remove oil from water. This system replaces the traditional dehydration section (three-phase separator, heater, electric dehydrator, oil-water buffer tank, etc.) and produced water treatment section (natural settling tank, coagulation settling tank, reactor, and water buffer tank, etc.) process routes. It solves the problems of large land area, long process flow, numerous equipment, high VOC emissions, and complex operation caused by the separate construction of produced water dehydration and water treatment sections in oilfields. Compared to the traditional process with more than 10 pieces of equipment, this produced fluid treatment process significantly reduces the number of operating equipment. This application provides a new process route and equipment. The incoming fluid only needs to pass through the efficient dehydration and water treatment equipment provided in this application to complete the dehydration and water treatment functions, achieving the effect that the produced oil can be directly exported, the produced water meets standards after filtration, and natural gas and other gases are collected and transported to the natural gas processing system.

[0071] Other features and advantages of this application will be set forth in the description which follows, and will be apparent in part from the description, or may be learned by practicing the application. Other advantages of this application may be realized and obtained by means of the methods described in the description. Attached Figure Description

[0072] The accompanying drawings are used to provide an understanding of the technical solutions of this application and constitute a part of the specification. They are used together with the embodiments of this application to explain the technical solutions of this application and do not constitute a limitation on the technical solutions of this application.

[0073] Figure 1 This is a schematic diagram of the conventional process flow for dehydration and water treatment of produced fluids in existing oilfields.

[0074] Figure 2 This is a schematic diagram of the integrated process for dehydration and water treatment of produced oil from the oilfield provided in this application.

[0075] Figure 3 This is a top-view schematic diagram of the internal partitions of the oilfield produced fluid dehydration and water treatment equipment provided in this application.

[0076] Figure 4 This is a top view schematic diagram of the structure of the oilfield produced fluid dehydration and water treatment equipment provided in this application.

[0077] Figure 5 The main view of the structure of the oilfield produced fluid dehydration and water treatment equipment provided in this application (i.e.) Figure 4 A cross-sectional diagram (viewed from the bottom to the top of the image).

[0078] Figure 6 The rear view of the structure of the oilfield produced fluid dehydration and water treatment equipment provided in this application (i.e.) Figure 4It is a schematic cross-sectional view viewed from the top to the bottom of the drawing.

[0079] Figure 7 It is a schematic cross-sectional view of the arrangement of inclined plate groups.

[0080] Figure 8 It is a schematic structural diagram of a Feng-shaped inclined plate.

[0081] Figure 9 It is a schematic top-view principle diagram of a Feng-shaped inclined plate.

[0082] Figure 10 It is a schematic diagram of a micro-vortex coalescence device.

[0083] Figure 11 It is a schematic diagram of the internal packing in the cross-section of the micro-vortex coalescence device.

[0084] Figure 12 It is a schematic diagram of the porous shell of the micro-vortex coalescence device.

[0085] 1. Dehydration and water treatment equipment for oilfield produced fluid; 1-1, density difference separation chamber; 1-11, cyclone separation chamber; 1-111, cyclone inlet of the equipment; 1-112, rake-type liquid distribution pipe; 1-113, rectifier plate; 1-114, gas outlet; 1-12, three-phase separation device; 1-121, coalescing inclined plate group; 1-122, first liquid outlet (water outlet (a1)); 1-123, second liquid outlet (oil receiving port (b)); 1-124, buffer weir plate;

[0086] 1-2, dielectric difference separation chamber; 1-21, oil outlet liquid distribution pipe (b); 1-22, grid electrode plate group; 1-23, oil outlet weir plate; 1-24, third liquid outlet (water outlet (a2)); 1-25, first gas outlet;

[0087] 1-3, buffer chamber; 1-31, oil outlet pipe of the equipment;

[0088] 1-4, enhanced oil removal chamber; 1-41, micro-vortex coalescence group; 1-410, first liquid inlet (water inlet (a)); 1-411, first micro-vortex coalescence chamber; 1-412, second micro-vortex coalescence chamber; 1-413, third micro-vortex coalescence chamber; 1-414, fourth micro-vortex coalescence chamber; 1-415, micro-vortex coalescence device; 1-4151, flow guide hole; 1-4152, coalescence packing; 1-4153, porous shell; 1-416, communicating pipe;

[0089] 1-42, inclined tube oil removal chamber; 1-421, uniform water distribution member; 1-422, downward flow inclined tube group; 1-423, fourth liquid outlet (water outlet (c)); 1-424, chemical feeding pipe; 1-425, oil sludge recovery pipe; 1-426, sludge discharge pipe;

[0090] 1-5, Suspended solid removal chamber; 1-51, Contact reaction group; 1-510, Second liquid inlet (water inlet (c)); 1-511, First contact reaction chamber; 1-512, Second contact reaction chamber; 1-513, Third contact reaction chamber; 1-514, Fourth contact reaction chamber; 1-515, Contact reaction promoting device (contact reaction ball); 1-516, Outlet weir plate;

[0091] 1-52, Inclined plate suspended solids removal chamber; 1-521, FENG-shaped inclined plate group; 1-5211, Support plate; 1-5212, Fins; 1-522, Uniform water distribution orifice plate; 1-523, Equipment water outlet;

[0092] 2, Filtration system; 2-1, Primary filter; 2-2, Secondary filter;

[0093] 3, Water purification tank; 4, Backwash recovered water tank; 5, Sludge tank; 6, Oil sludge tank; 7, External water delivery pump; 8, Backwash pump; 9, Backwash water reflux pump; 10, Dirty oil reflux pump; 11, Purified oil external delivery pump; 12, Demulsifier feeding port; 13, Coagulant and flocculant feeding port; 14, Pipeline for conveying to natural gas processing system. Detailed Description of Embodiments

[0094] To make the objectives, technical solutions and advantages of the present application clearer, the embodiments of the present application are described in detail below. It should be noted that, without conflict, the embodiments in the present application and the features in the embodiments can be arbitrarily combined with each other.

[0095] Figure 1 is a schematic diagram of a conventional process flow for dewatering produced liquid from existing oilfields and water treatment. Figure 2 is a schematic diagram of the integrated process for dewatering produced liquid from oilfields and water treatment provided by the present application. Figure 3 is a top schematic view of the internal partition of the equipment for dewatering produced liquid from oilfields and water treatment provided by the present application. Figure 4 is a top structural schematic view of the equipment for dewatering produced liquid from oilfields and water treatment provided by the present application. Figure 5 is a cross-sectional schematic view of the structure of the equipment for dewatering produced liquid from oilfields and water treatment provided by the present application in the front view direction (i.e., Figure 4 viewing from the bottom to the top of the drawing). Figure 6 is a cross-sectional schematic view of the structure of the equipment for dewatering produced liquid from oilfields and water treatment provided by the present application in the rear view direction (i.e., Figure 4 viewing from the top to the bottom of the drawing). Figure 7 is a cross-sectional schematic view of the arrangement of inclined plate groups. Figure 8 is a structural schematic view of the FENG-shaped inclined plate. Figure 9 is a top schematic view of the working principle of the FENG-shaped inclined plate. Figure 10 is a schematic view of the micro-vortex coalescence device. Figure 11This is a schematic diagram of the packing material inside the micro vortex coalescing device. Figure 12 This is a schematic diagram of the porous shell of a micro-vortex coalescing device.

[0096] like Figures 1 to 11 As shown, this application provides an oilfield produced fluid dehydration and water treatment device 1, comprising:

[0097] The first chamber includes a density difference separation chamber 1-1, a dielectric difference separation chamber 1-2, and a buffer chamber 1-3; the second chamber includes an enhanced degreasing chamber 1-4 and a suspended solids removal chamber 1-5.

[0098] The first chamber and the second chamber form a can-shaped structure; the aspect ratio of the can-shaped structure is 3 to 6.

[0099] The density difference separation chamber 1-1 is configured to perform oil-water separation and / or solid-liquid separation by utilizing the density difference of the oilfield produced fluid.

[0100] The dielectric difference separation chamber 1-2 is configured to perform oil-water separation and / or solid-liquid separation by dielectric difference;

[0101] The enhanced oil removal chambers 1-4 are configured to perform oil-water separation and / or solid-liquid separation through any one or more of micro-vortex coalescence and density difference.

[0102] The suspended solids removal chambers 1-5 are configured to perform oil-water separation and / or solid-liquid separation by any one or more of flocculation reaction and / or density difference.

[0103] For example, such as Figure 4 and Figure 5 As shown, the density difference separation chamber 1-1 is equipped with a liquid inlet device (i.e., cyclone separation chamber 1-11), a three-phase separation device 1-12, a first liquid outlet (water outlet (a1)) 1-122, and a second liquid outlet (oil collection outlet (b)) 1-123.

[0104] For example, such as Figure 4 and Figure 5 As shown, the liquid inlet device (i.e., the cyclone separation chamber 1-11) is configured to separate the gas phase and the liquid phase by cyclone separation, including a cyclone liquid inlet device (i.e., the equipment cyclone liquid inlet 1-111), a rake-type liquid distribution pipe 1-112 and a rectifier plate 1-113;

[0105] The three-phase separation device 1-12 includes a coalescing inclined plate group 1-121; the coalescing inclined plate group 1-121 is a group composed of coalescing inclined plates;

[0106] For example, such as Figure 4 and Figure 6As shown, the dielectric differential separation chamber 1-2 is provided with a grid-type electrode plate group 1-22, a first gas outlet 1-25 and a third liquid outlet (water outlet (a2)) 1-24.

[0107] For example, such as Figure 4 and Figure 5 As shown, the enhanced oil removal chamber 1-4 is provided with at least one micro vortex coalescence chamber and at least one inclined tube oil removal chamber 1-42.

[0108] The micro vortex coalescence chamber and the inclined tube oil removal chamber 1-42 are configured such that liquid flows sequentially through the micro vortex coalescence chamber and the inclined tube oil removal chamber 1-42;

[0109] The micro vortex coalescing chamber is equipped with a first liquid inlet (water inlet (a)) 1-410 and a micro vortex coalescing device 1-415;

[0110] There are two or more micro vortex coalescing chambers, and the liquid flowing out of the first liquid inlet (water inlet (a)) 1-410 passes through all the micro vortex coalescing chambers in sequence;

[0111] The inclined tube oil removal chamber 1-42 is equipped with a downward flow inclined tube group 1-422 and a fourth liquid outlet (water outlet (c)) 1-423.

[0112] For example, such as Figure 4 and Figure 5 As shown, the first liquid outlet (water outlet a1) and the third liquid outlet (water outlet (a2)) are connected to the first liquid inlet (water inlet (a)) 1-410.

[0113] For example, such as Figure 4 and Figure 6 As shown, the suspended solids removal chamber 1-5 is provided with at least a contact reaction chamber and an inclined plate desuspension chamber 1-52.

[0114] The contact reaction chamber and the inclined plate desuspension chamber 1-52 are configured such that liquid flows sequentially through the contact reaction chamber and the inclined plate desuspension chamber 1-52;

[0115] For example, such as Figure 4 and Figure 6 As shown, the contact reaction chamber is provided with at least a second liquid inlet (water inlet (c)) 1-510 and a contact reaction promoting device (contact reaction ball) 1-515;

[0116] There are two or more contact reaction chambers, and the liquid flowing out of the second liquid inlet (water inlet (c)) 1-510 passes through all the contact reaction chambers in sequence;

[0117] The inclined plate suspension removal chamber 1-52 is provided with at least a Feng-shaped inclined plate group 1-521 and an equipment water outlet 1-523, and the liquid flowing through the Feng-shaped inclined plate group 1-521 flows out of the oilfield produced liquid dehydration and water treatment equipment from the equipment water outlet 1-523.

[0118] For example, as Figure 4 and Figure 6 shown, the fourth liquid outlet (water outlet (c)) 1-423 is in communication with the second liquid inlet (water inlet (c)) 1-510;

[0119] For example, as Figure 4 and Figure 6 shown, the fourth liquid outlet (water outlet (c)) 1-423 is in communication with the second liquid inlet (water inlet (c)) 1-510, and a chemical feeding pipe 1-424 is further arranged on the pipeline between the fourth liquid outlet (water outlet (c)) 1-423 and the second liquid inlet (water inlet (c)) 1-510.

[0120] For example, as Figure 4 shown, the density difference separation chamber 1-1 in the first chamber is adjacent to the dielectric difference separation chamber 1-2 in the second chamber;

[0121] A buffer weir plate 1-124 is arranged between the density difference separation chamber 1-1 and the dielectric difference separation chamber 1-2;

[0122] The buffer weir plate 1-124 is configured such that when the liquid level in the density difference separation chamber 1-1 is higher than the top of the buffer weir plate 1-124, the low-density liquid in the density difference separation chamber 1-1 flows over the buffer weir plate 1-124 and enters the dielectric difference separation chamber 1-2.

[0123] For example, as Figures 7 to 9 shown, the Feng-shaped inclined plate group 1-521 is composed of a plurality of Feng-shaped inclined plates, and the Feng-shaped inclined plates comprise wing plates 1-5212 and support plates 1-5211 supporting the wing plates 1-5212; Figure 7 it is a cross-sectional view of the tank body where the viewing direction of the Feng-shaped inclined plate group 1-521 and the downward flow inclined tube group is perpendicular to the ground direction, Figure 7 the water flow direction therein flows in a direction perpendicular to the paper surface.

[0124] the wing plates 1-5212 are configured to hinder the fluid in the Feng-shaped inclined plate group 1-521 from flowing along the length direction of the support plates 1-5211.

[0125] In an embodiment provided by the present application, the Feng-shaped inclined plate is configured such that the movement direction of the fluid flowing through the Feng-shaped inclined plate forms an angle of 45° to 80° with the horizontal plane.

[0126] For example, as Figures 7 to 9 As shown, the ratio of the spacing between adjacent winglets 1-5212 to the height of winglet 1-5212 (the height of winglet 1-5212 is the length of winglet 1-5212 perpendicular to the length direction of support plate 1-5211) is (10 to 60):(10 to 60); the height of winglet 1-5212 can be 10mm to 60mm.

[0127] For example, such as Figures 7 to 9 As shown, the ratio of the height of the wing 1-5212 to the distance between two adjacent support plates 1-5211 is (10 to 60):(40 to 150).

[0128] For example, such as Figure 10 , Figure 11 and Figure 12 As shown, the micro-vortex coalescing group 1-41 comprises multiple micro-vortex coalescing chambers, and includes a micro-vortex coalescing device 1-415; the micro-vortex coalescing device 1-415 is a porous shell 1-4153 (i.e., a micro-vortex coalescing sphere) filled with coalescing packing material 1-4152, and the micro-vortex coalescing device 1-415 has a hollow structure, comprising:

[0129] Porous shell 1-4153 (i.e., micro vortex coalescing sphere); the porous shell 1-4153 is provided with a guide hole 1-4151 that connects the inside and outside of the micro vortex coalescing device 1-415;

[0130] The coalescing packing 1-4152 is disposed in the hollow structure.

[0131] The longest diameter of the guide hole 1-4151 is smaller than the shortest diameter of the coalescing packing 1-4152.

[0132] For example, the flow guide holes 1-4151 occupy 30% to 80% of the area of ​​the porous housing 1-4153.

[0133] For example, the micro vortex coalescing device 1-415 is a sphere; for example, the ratio of the outer diameter of the micro vortex coalescing device 1-415 to the thickness of the porous shell 1-4153 is (100 to 300):(1 to 6); for example, the ratio of the outer diameter of the micro vortex coalescing device 1-415 to the diameter-to-length ratio of the guide hole 1-4151 is (100 to 300):(15 to 40).

[0134] For example, such as Figure 10 , Figure 11 and Figure 12 As shown, a plurality of coalescing packings 1-4152 in a micro vortex coalescing device 1-415 have space for rotational movement within a porous housing 1-4153.

[0135] For example, the material of the porous shell 1-4153 may be selected from any one or more plastic materials such as ABS, modified ABS, polypropylene, modified polypropylene and polyethylene.

[0136] For example, the material of the coalescing filler 1-4152 can be selected from any one or more plastic materials such as ABS, modified ABS, polypropylene, modified polypropylene and polyethylene.

[0137] For example, the length ratio of the outer diameter of the micro vortex coalescing device 1-415 to the outer diameter of the coalescing packing 1-4152 is 1:(0.125 to 0.5).

[0138] For example, the outer diameter of the micro vortex coalescing device 1-415 can be from 100 mm to 300 mm.

[0139] For example, the outer diameter of the coalescing packing 1-4152 can be from 25 mm to 75 mm. For example, the outer diameter of the coalescing packing 1-4152 is larger than the diameter of the flow guide hole.

[0140] For example, the coalescing packing 1-4152 is selected from any one or more of Pall ring packing, stepped ring packing, rectangular saddle ring packing, multifaceted hollow ball packing, hollow ball packing, porous ball packing, Raschig ring packing, heterosaddle ring packing and gear ring packing.

[0141] For example, the average material density of the micro eddy current coalescing device 1-415 is 0.90 × 10⁻⁶. 3 kg / m 3 Up to 1.1×10 3 kg / m 3 .

[0142] For example, such as Figure 4 and Figure 6 As shown, an oil weir plate 1-23 is provided between the buffer chamber 1-3 and the dielectric differential separation chamber 1-2;

[0143] The oil outlet weir plate 1-23 is configured such that liquid with a lower density than the oil outlet weir plate 1-23 in the dielectric differential separation chamber 1-2 overflows the oil outlet weir plate 1-23 and enters the buffer chamber 1-3.

[0144] For example, such as Figure 4 , Figure 5 and Figure 6As shown, the dielectric difference separation chamber 1-20 is connected to the enhanced oil removal chamber 1-4 via a pipeline, and the enhanced oil removal chamber 1-4 is connected to the suspended solids removal chamber 1-5. This allows the liquid, after entering the oilfield produced fluid dehydration and water treatment equipment 1, to flow sequentially through the density difference separation chamber 1-1, the dielectric difference separation chamber 1-2, the enhanced oil removal chamber 1-4, and the suspended solids removal chamber 1-5 before exiting. Oil in the liquid flows out through a buffer chamber outlet device.

[0145] For example, the direction of fluid movement in the micro-vortex coalescing chamber is perpendicular to the length direction of the can-shaped structure;

[0146] For example, the direction of fluid movement in the contact reaction chamber is perpendicular to the length direction of the tank-like structure;

[0147] For example, the direction of fluid movement in the micro-vortex coalescence chamber and the contact reaction chamber is perpendicular to the length direction of the canister structure.

[0148] On another front, this application provides a method for dehydrating and treating oilfield produced fluids, using the aforementioned oilfield produced fluid dehydration and water treatment equipment, comprising:

[0149] The residence time in the density difference separation chamber 1-1 is 15 min to 90 min, the residence time can be 15-45 min, and the residence time can also be 30 min to 45 min;

[0150] The residence time of the dielectric differential separation cavity 1-2 is 10 min to 90 min, preferably 30 min to 45 min;

[0151] The residence time in the enhanced degreasing chambers 1-4 is 20 min to 90 min, preferably 35 min to 40 min;

[0152] The residence time of the suspended solid removal chambers 1-5 is 15 min to 90 min, preferably 30 min to 40 min;

[0153] The residence time in the oil buffer chamber is 10 min to 60 min, preferably 10 min to 20 min;

[0154] For example, the oilfield produced fluid dehydration and water treatment equipment outputs purified oil with a water content of less than 0.5%, and the gas separated from the produced fluid contains produced water with an oil content and suspended solids content of less than 50 mg / L.

[0155] For example, such as Figure 2 As shown, the above-mentioned oilfield produced fluid dehydration and water treatment equipment 1, as well as the filtration system 2, clean water tank 3, backwash recovery water tank 4, sludge tank 5 and sludge oil tank 6 are used.

[0156] After the oilfield produced fluid is treated with a demulsifier, it enters the oilfield produced fluid dehydration and water treatment equipment 1 to separate gas, purified oil, produced water and sludge.

[0157] The gas is transported to the natural gas processing system, the purified oil is directly transported out from the buffer chamber 3 through the pipeline, and the produced water is stored and transported out after passing through a single-stage or multi-stage filtration (the primary filter 2-1 and the secondary filter 2-2 in the filtration system 2). The backwash water obtained by the backwashing device used for producing water filtration enters the backwash recovery water tank 4 and flows back to the enhanced oil removal chamber 1-4 of the oilfield produced fluid dehydration and water treatment equipment 1.

[0158] The sludge collected in the enhanced oil removal chambers 1-4 is stored in the sludge tank 6 and then returned to the oilfield produced fluid inlet of the oilfield produced fluid dehydration and water treatment equipment 1. The sludge separated by the oilfield produced fluid dehydration and water treatment equipment 1 is stored in the sludge tank and transported off-site for treatment.

[0159] The specific implementation plan for oilfield produced fluid dehydration and water treatment process is as follows:

[0160] A demulsifier dosing port 12 is installed on the oilfield well produced fluid pipeline. After being mixed in the pipeline, the fluid enters the produced fluid dehydration and water treatment equipment 1. After three-phase separation, dehydration and water treatment in the produced fluid dehydration and water treatment equipment 1, the separated gas is transported to the natural gas processing system via pipeline 14. The separated purified oil is transported to the outside via purified oil external pump 11. The separated produced water enters the filtration system 2. After passing through primary filtration 2-1 and secondary filtration 2-2, it enters the clean water tank 3. The purified water is transported to the outside via external water pump 7.

[0161] The water treatment section of the produced fluid dehydration and water treatment equipment 1 is equipped with coagulant and flocculant dosing ports 13 for the removal of suspended solids in the water treatment section.

[0162] The waste oil collected in the water treatment section of the equipment is recycled to the waste oil tank 6 by pipeline, and the waste oil is transported to the front end of the produced fluid dehydration and water treatment equipment 1 by the waste oil return pump 10.

[0163] The sludge produced by the produced fluid dewatering and water treatment equipment 1 (such as the sludge discharged from the sludge discharge pipes 1-426) is discharged from the bottom of the equipment into the sludge tank 5 and transported off-site for treatment on a regular basis.

[0164] During the backwashing operation of the filtration system 2, the backwash water is transported from the clean water tank 3 to the filtration system 2 via the backwash pump 8. The backwash wastewater is discharged into the backwash recovery water tank 4 and then transported back to the water treatment section of the produced fluid dehydration and water treatment equipment 1 via the backwash water return pump 9.

[0165] like Figures 4 to 6 As shown, the specific implementation plan for the produced fluid in the dehydration and water treatment equipment is as follows:

[0166] 1) The incoming liquid enters through the cyclone inlet 1-111 of the produced liquid dewatering and water treatment equipment 1. After preliminary separation of the gas and liquid phases by cyclone separation, the gas phase is discharged from the gas outlet 1-114, and the liquid enters the cyclone separation chamber 1-11 through the rake-type liquid distribution pipe 1-112; inlet conditions: temperature 50℃, pressure 0.3MPa, liquid flow rate 500m³. 3 / d, water content 50%, gas-oil ratio 100m 3 / t;

[0167] 2) Water is evenly distributed in the water through the rake-type liquid distribution pipe 1-112, and liquid is introduced from the water layer to achieve enhanced water washing. The rake-type liquid distribution pipe 1-112 has two sets of three distribution pipes each. Each distribution pipe has 13 evenly distributed distribution holes at the top and 7 evenly distributed distribution holes at the bottom, all with a diameter of 10mm. The rake-type liquid distribution pipe is less likely to generate vortices.

[0168] 3) After flowing through the rectifier plate 1-113, the liquid enters the three-phase separation device 1-12. This three-phase separation device is a conventional three-phase separation device in the art, relying on density difference for gas-liquid separation. Oil and water are separated after rectification and coalescence. a) Gas-liquid separation: Gas is discharged from the upper first gas outlet 1-25. The gas-liquid interface is at 3 / 4 of the container diameter, allowing for the separation of 100μm liquid droplets from the gas. b) The rectifier plate 1-113 has an orifice plate configuration with an opening rate of 30%, and is 800mm from the inlet centerline, achieving uniform water distribution. c) The coalescence inclined plate assembly 1-121 is made of fiber-reinforced composite material, separating oil and water through coalescence collision. This coalescence inclined plate assembly is a conventional coalescence inclined plate in the art. d) Free water is discharged from the first outlet (outlet (a1)) 1-122 at the lower end to the first inlet (inlet (a)) of the enhanced oil removal chamber 1-4; water-containing oil enters the dielectric differential separation chamber 1-2 through the second outlet (oil receiving outlet (b)) 1-123 located at the top of the liquid level in the three-phase separation chamber. e) When the incoming liquid flow rate is less than or equal to the equipment design flow rate, the water-containing oil passes through the dielectric differential separation chamber 1-2 via the oil receiving outlet (b) 1-123 and the oil distribution pipe (b) 1-21. When the incoming liquid flow rate exceeds the design flow rate, the liquid level in the density difference separation chamber 1-1 rises, and the water-containing oil can directly cross over to the dielectric differential separation chamber 1-2 through the buffer weir plate 1-124 for the next step of dehydration.

[0169] 4) After the water-containing oil flows into the second outlet (oil receiving port (b)) 1-123, it flows into the dielectric differential separation chamber 1-2 through the oil distribution pipe (b) 1-21. Under the action of the high-frequency electric field of the grid-type electrode plate group 1-22 (a total of four electrode plates, of which the second and third electrode plates are connected to the tank body), the water-in-oil emulsion is demulsified, coalesced, and then settled and separated. The oil is discharged into the buffer chamber 3 through the oil weir plate 1-23, and the free water is discharged from the lower third outlet (water outlet (a2)) 1-24 to the first inlet (water inlet (a)) 1-410 of the enhanced oil removal chamber 1-4.

[0170] 5) The purified oil is evenly discharged from the buffer chamber 3 through the equipment oil outlet pipes 1-31. Oily wastewater enters the enhanced oil removal chamber 1-4 from the first inlet (inlet (a)) 1-410, and then enters the first micro-vortex coalescing chamber 1-411 equipped with several micro-vortex coalescing devices 1-415. The water flows from bottom to top, passing through several micro-vortex coalescing devices 1-415. When the wastewater flows through the micro-vortex coalescing devices, collision coalescing and wetting coalescing occur, causing the oil droplets to grow from small to large and float to the surface. The micro-vortex coalescing chambers are connected by a connecting pipe 1-416, and the water flows from the top to the bottom through the connecting pipe 1-416, entering the second micro-vortex coalescing chamber 1-412 and flowing upward again, repeating the process of the first micro-vortex coalescing chamber. Then, it enters the third micro-vortex coalescing chamber 1-413 and the fourth micro-vortex coalescing chamber 1-414 in sequence. After passing through the four micro-vortex coalescing chambers, it flows out horizontally from the uniform water distribution component 1-421 above the inclined tube oil removal chamber 1-42.

[0171] 6) The inclined tube oil removal section 1-42 is a downward flow section. After the wastewater flows horizontally and evenly from above the inclined tube oil removal chamber 1-42, it enters the downward flow inclined tube group 1-422 in the inclined tube area. The probability of oil droplet collision is increased in the inclined tube. At the same time, the oil is naturally removed by utilizing the density difference between oil and water. The oil droplets collide and aggregate into large oil droplets in the water flow and float to the surface. It mainly removes floating oil and dispersed oil larger than 50μm. The inclined tube is a conventional inclined tube in this field. After passing through the downward flow inclined tube group 1-422, the water flow is transported from the fourth liquid outlet (water outlet (c)) 1-423 to the second liquid inlet (water inlet (c)) 1-510 of the suspended solids removal chamber 1-5.

[0172] 7) A dosing pipe 1-424 is provided in the pipeline leading to the suspended solids removal chamber 1-5. Coagulants and flocculants are mainly added and quickly mixed in the pipeline. The water then exits from the bottom of the first contact reaction chamber 1-511 of the suspended solids removal chamber 1-5.

[0173] 8) The sewage uniformly mixed with the medicament enters the first contact reaction chamber 1-511 provided with a plurality of contact reaction balls 1-515. When flowing through the contact reaction balls (the contact reaction ball is a porous shell, which is a micro-vortex coalescence device excluding coalescing packing) 1-515, the collision contact probability between the medicament and suspended solids is increased, flocs are gradually formed, and a suspended floc layer is formed. Said floc layer has a strong adsorption effect, and continuously adsorbs fine particles, thereby making the flocs continuously larger. Larger flocs settle, while smaller flocs follow the water flow into the communicating pipe and lead to the second contact reaction chamber 1-512, where a flocculation contact reaction is carried out again, and then pass through the third contact reaction chamber 1-513 and the fourth contact reaction chamber 1-514 in sequence. The water flow containing flocs flows out from the effluent weir plate 1-516 of the fourth contact reaction chamber 1-514.

[0174] 9) The outflow water enters the inclined plate suspended matter removal chamber 1-52, passes through a uniform water distribution orifice plate 1-522, and enters the丰-shaped inclined plate group 1-521. In the丰-shaped inclined plate group 1-521, the water flow direction flows perpendicularly to the fins 1-5212. The water flow is disturbed at the edge of the fins 1-5212 to change the local water flow direction and form a micro-vortex area, while the water flow that is not disturbed or less disturbed by the fins 1-5212 will continue to flow forward between the inclined plates, and this part of less disturbed water flow is the main flow area. A part of the water flow close to the fins 1-5212 that is disturbed will form a vortex, forming a vortex area; the water flow in the vortex area enters between two fins 1-5212, and under a certain flow rate maintained in the main flow area, a local circulation will be formed between the fins 1-5212. Oil droplets rise in the water flow, and suspended solids settle in the water flow. When oil droplets or suspended solids are rising and falling, the oil droplets enter the micro-vortex area of the upper fins of the water flow, and the suspended solids enter the micro-vortex area of the lower fins of the water flow, and then are entrained into the circulation area adjacent to the fin respectively. In the circulation area between the fin grids, both oil droplets and suspended solids have enough space and reaction time for collision coalescence and sedimentation. After collision coalescence, the oil droplets float upward along the fins, and the suspended solids descend spirally between the fin grids, settle to the inclined plate surface and slide down to be removed. For conventional lateral flow inclined plates, after oil droplets float to the top inclined plate of the water flow or suspended solids settle to the bottom inclined plate of the water flow, the oil droplets and suspended solids are affected by the partial velocity of the water flow, the collision probability between oil droplets and between suspended solids is low, and the probability of secondary escape of oil droplets and suspended solids affected by the water flow is relatively high, resulting in low oil removal efficiency. The丰-shaped inclined plate group 1-521 is conducive to simultaneously removing suspended solids and oil, ensuring the treatment effect. After exiting from the丰-shaped inclined plate group 1-521, the water flow passes through the uniform water distribution orifice plate 1-522 again, and flows out through the equipment water outlet 1-523.

[0175] 10) The equipment is equipped with a sludge discharge pipe 1-426 for discharging sediment and sludge during dewatering and water treatment. The water treatment section (enhanced oil removal chamber 1-4 and suspended solids removal chamber 1-5) is equipped with a sludge oil collection pipe 1-425 to collect the sludge oil on the liquid surface and discharge it outside the equipment to the sludge oil tank 6. Water from the backwash recovery water tank is treated outside the equipment and enters from the first liquid inlet (inlet (a)).

[0176] 11) After the oilfield produced fluid passes through the density difference separation chamber 1-1, the dielectric difference separation chamber 1-2, the enhanced oil removal chamber 1-4, and the suspended solids removal chamber 1-5, the wastewater quality reaches an oil content and suspended solids content of less than 50 mg / L. Utilizing the residual self-pressure of the pressure equipment, it can directly flow into the next stage filtration system 2.

[0177] Technical effects:

[0178] 1) Shortened process: Compared with the traditional dehydration and water treatment process, the integrated process system for dehydration and water treatment of oilfield produced fluid has greatly shortened the process. The original equipment of more than 10 stages for dehydration and water treatment has been reduced to a single main equipment and supporting facilities, which has greatly optimized and improved the process in terms of land occupation, operation, maintenance and management.

[0179] 2) Comprehensive Functions: The oilfield produced fluid dehydration and water treatment equipment is internally divided into four blocks and one buffer chamber. The four blocks are functionally defined as follows: ① density difference dehydration zone, ② dielectric difference deep dehydration zone, ③ enhanced oil removal zone, and ④ suspended solids removal zone. Through ingenious design and layout, the equipment ensures that the oil water content in the produced fluid dehydration and water treatment equipment is below 0.5%, and the oil content and suspended solids content in the effluent are below 50 mg / L. With the addition of subsequent filters, the water quality can meet even stricter requirements.

[0180] 3) Reasonable Length-to-Diameter Ratio: The length-to-diameter ratio is the ratio of the equipment's length to its width. Traditional horizontal tank skid-mounted integrated equipment is mostly divided into chambers from front to back. If many technologies are used, a certain range of length-to-diameter ratio needs to be maintained to ensure that the processing effect is not affected. For example, processes such as three-phase separators and electric dehydrators result in a large length-to-diameter ratio of the integrated equipment, sometimes reaching 7 to 10 or more. The overall equipment is long and thin, which is inconvenient for manufacturing, transportation, and on-site layout, and also increases the footprint. The oilfield produced fluid dehydration and water treatment equipment adopts a left-right chamber design. Combined with the layout, the length-to-diameter ratio is reduced, and the footprint is reduced. This solves the problem of excessive length-to-diameter ratio of skid-mounted integrated equipment. The equipment's length-to-diameter ratio is around 4, similar to that of ordinary horizontal tank equipment, improving the feasibility and convenience of manufacturing, transportation, and on-site layout.

[0181] 4) Energy Saving: In traditional dehydration processes, the incoming liquid needs to be kept at a certain temperature, generally between 30°C and 50°C, to ensure the dehydration effect. If the temperature is not reached, heating or additional insulation measures are required. By eliminating the pipeline links between equipment, the produced fluid can be directly and rapidly transferred short distances within the oilfield produced fluid dehydration and water treatment equipment, reducing the loss of liquid temperature during transportation and achieving the effect of saving heating energy.

[0182] 5) Shared Buffer: Traditional dehydration and water treatment processes typically use 3 to 5 buffer tanks to regulate the uniform delivery of liquid to the next stage. Oilfields with poor water quality or large fluctuations may require even more, leading to longer processes, larger footprints, and higher investment costs. In our oilfield produced fluid dehydration and water treatment equipment, only one oil buffer chamber is installed. Oil from the dehydration zone can be directly delivered to the buffer chamber via a weir after separation, thus solving the problems caused by multiple buffer tanks in traditional processes while maintaining the buffer regulation function.

[0183] 6) Self-pressurized pump replacement: In traditional dehydration and water treatment processes, if the pressure between equipment is insufficient, oil or water needs to be pumped to boost the flow. Using more pumps not only increases investment and power consumption, but also intensifies the emulsification of the produced fluid due to the violent agitation of the pump impeller, making oil-water separation more difficult and increasing the residence time. The oilfield produced fluid dehydration and water treatment equipment provided in this application is a pressure-type device. The internal blocks rely on inlet pressure for continuous self-pressurized flow. The water separated in the oil removal zone directly enters the primary filter under residual pressure, eliminating the need for additional pumps. This saves energy while improving the efficiency of oil-water separation.

[0184] 7) Short residence time: The total hydraulic residence time of traditional dehydration and water treatment is more than 7 to 8 hours, while the oilfield produced fluid dehydration and water treatment equipment provided in this application only requires 2 to 3 hours. The purified oil can be exported, and the purified water can be exported after passing through the filter, which greatly improves the treatment efficiency.

[0185] 8) Reduction of VOCs emissions: Traditional dehydration and water treatment processes involve a large number of equipment and buffer tanks. During the crude oil buffer tank, purified oil storage tank and produced water transportation and treatment, a large amount of VOCs will escape and cause pollution. However, the oilfield produced fluid dehydration and water treatment equipment provided in this application adopts skid-mounted pressurized treatment and is equipped with a dedicated exhaust pipeline. The equipment has no VOCs emissions, achieving the purpose of environmental protection and safety.

[0186] 9) Fewer Supporting Facilities: Traditional dehydration and water treatment processes require numerous pipeline connections and valve controls, which not only increases investment and maintenance costs but also poses risks of contamination such as iron bacteria in the pipelines, localized pressure losses due to valves, and safety and environmental problems caused by pipeline and valve leaks. The oilfield produced fluid dehydration and water treatment equipment provided in this application requires only a small number of pipeline connections and valve controls. The entire equipment can be inspected and maintained uniformly, greatly reducing the risks of leaks and secondary pollution.

Claims

1. An oilfield produced fluid dehydration and water treatment device, characterized in that, Comprising: a first chamber and a second chamber, wherein the first chamber comprises a density difference separation cavity, a dielectric difference separation cavity and a buffer cavity; the second chamber comprises an enhanced oil removal cavity and a suspended solid removal cavity; the first chamber and the second chamber form a tank-shaped structure; and the length-to-diameter ratio of the tank-shaped structure is 3 to 6; the density difference separation cavity is configured to perform oil-water separation and / or solid-liquid separation through the density difference of oilfield produced fluid; the dielectric difference separation cavity is configured to perform oil-water separation and / or solid-liquid separation through dielectric difference; the enhanced oil removal cavity is configured to perform oil-water separation and / or solid-liquid separation through any one or more of micro-vortex coalescence and density difference; the suspended solid removal cavity is configured to perform oil-water separation and / or solid-liquid separation through any one or more of flocculation reaction and / or density difference; a liquid inlet device, a three-phase separation device, a first liquid outlet and a second liquid outlet are arranged in the density difference separation cavity; an electrode plate group, a first gas outlet and a third liquid outlet are arranged in the dielectric difference separation cavity; at least one micro-vortex coalescing chamber and at least one inclined tube oil removal chamber are arranged in the enhanced oil removal cavity; the suspended solid removal cavity is at least provided with a contact reaction chamber and an inclined plate suspended solids removal chamber; the inclined plate suspended solids removal chamber is at least provided with a #-shaped inclined plate group and an equipment water outlet; the #-shaped inclined plate group consists of a plurality of #-shaped inclined plates; the #-shaped inclined plate comprises fins and support plates for supporting the fins; the fins are configured to hinder fluid in the #-shaped inclined plate group from flowing along the length direction of the support plates; the ratio of the height of the fin to the spacing between two adjacent support plates is (10 to 60):(40 to 150).

2. The oilfield produced fluid dehydration and water treatment equipment according to claim 1, characterized in that, the liquid inlet device is configured to separate gas phase and liquid phase through swirling, and comprises a swirling liquid inlet device, a rake type liquid distribution pipe and a flow rectifying plate; a coalescing inclined plate group is included in the three-phase separation device.

3. The oilfield produced fluid dehydration and water treatment equipment according to claim 1 or 2, characterized in that, the micro-vortex coalescing chamber and the inclined tube oil removal chamber are configured such that liquid flows through the micro-vortex coalescing chamber and the inclined tube oil removal chamber in sequence; a first liquid inlet and a micro-vortex coalescing device are arranged in the micro-vortex coalescing chamber; there are two or more micro-vortex coalescing chambers, and the liquid flowing out from the first liquid inlet passes through all the micro-vortex coalescing chambers in sequence; a downward flow inclined tube group and a fourth liquid outlet are arranged in the inclined tube oil removal chamber.

4. The oilfield produced fluid dehydration and water treatment equipment according to claim 3, characterized in that, the second liquid outlet and the third liquid outlet are communicated with the first liquid inlet.

5. The oilfield produced fluid dehydration and water treatment equipment according to claim 3, characterized in that, the contact reaction chamber and the inclined plate suspended solids removal chamber are configured such that liquid flows through the contact reaction chamber and the inclined plate suspended solids removal chamber in sequence; the contact reaction chamber is at least provided with a second liquid inlet and a device for promoting contact reaction; there are two or more contact reaction chambers, and the liquid flowing out from the second liquid inlet passes through all the contact reaction chambers in sequence.

6. The oilfield produced fluid dehydration and water treatment equipment according to claim 5, characterized in that, the fourth liquid outlet is communicated with the second liquid inlet; alternatively, the fourth liquid outlet is communicated with the second liquid inlet; and a chemical feeding pipe is further arranged on a pipeline between the fourth liquid outlet and the second liquid inlet.

7. The oilfield produced fluid dehydration and water treatment equipment according to claim 1 or 2, characterized in that, the density difference separation cavity in the first chamber is adjacent to the dielectric difference separation cavity in the first chamber; a buffer weir plate is arranged between the density difference separation cavity and the dielectric difference separation cavity; The buffer weir is configured such that the liquid level in the density difference separation chamber is higher than the top of the buffer weir, and the liquid in the density difference separation chamber overflows the buffer weir and enters the dielectric difference separation chamber.

8. The oilfield produced fluid dehydration and water treatment equipment according to claim 1 or 2, characterized in that, The inclined plate is configured such that the direction of fluid flow through the inclined plate is at an angle of 45° to 80° with the horizontal plane.

9. The oilfield produced fluid dehydration and water treatment equipment according to claim 1 or 2, characterized in that, The ratio of the spacing between adjacent winglets to the height of the winglet is (10 to 60):(10 to 60).

10. The oilfield produced fluid dehydration and water treatment equipment according to claim 1 or 2, characterized in that, The micro vortex coalescing chamber includes a micro vortex coalescing device; the micro vortex coalescing device is a micro vortex coalescing ball filled with coalescing packing, and the length ratio of the outer diameter of the micro vortex coalescing ball to the outer diameter of the coalescing packing is 1:(0.125 to 0.5).

11. The oilfield produced fluid dehydration and water treatment equipment according to claim 10, characterized in that, The micro-vortex coalescing chamber contains micro-vortex coalescing spheres with a diameter of 100mm to 300mm, and is filled with coalescing packing material with a diameter of 25mm to 75mm.

12. The oilfield produced fluid dehydration and water treatment equipment according to claim 10, characterized in that, The average density of the material in the micro-vortex coalescing device in the micro-vortex coalescing chamber is 0.90 × 10⁻⁶. 3 kg / m 3 Up to 1.1×10 3 kg / m 3 .

13. The oilfield produced fluid dehydration and water treatment equipment according to claim 1 or 2, characterized in that, An oil weir plate is provided between the buffer chamber and the dielectric differential separation chamber; The oil outlet weir plate is configured such that liquid in the dielectric differential separation chamber that is above the oil outlet weir plate overflows the oil outlet weir plate and enters the buffer chamber.

14. The oilfield produced fluid dehydration and water treatment equipment according to claim 1 or 2, characterized in that, The dielectric differential separation chamber is connected to the enhanced degreasing chamber via a pipeline, and the enhanced degreasing chamber is connected to the suspended solids removal chamber.

15. The oilfield produced fluid dehydration and water treatment equipment according to claim 5, characterized in that, The direction of fluid movement in the micro-vortex coalescence chamber is perpendicular to the length direction of the canister structure. Alternatively, the direction of fluid movement in the contact reaction chamber is perpendicular to the length direction of the tank-like structure; Alternatively, the direction of fluid movement in the micro-vortex coalescence chamber and the contact reaction chamber is perpendicular to the length direction of the canister structure.

16. A method for dehydrating and treating produced fluid from an oilfield, characterized in that, The oilfield produced fluid dehydration and water treatment equipment according to any one of claims 1 to 15 includes: The residence time in the density difference separation chamber is 15 min to 90 min; The residence time of the dielectric differential separation cavity is 10 min to 90 min; The residence time in the enhanced degreasing chamber is 20 min to 90 min; The residence time in the cavity for removing suspended solids is 15 min to 90 min; The residence time in the buffer chamber is 10 to 60 minutes.

17. The method for dehydrating and treating produced oil from oilfields according to claim 16, characterized in that, Use the oilfield produced fluid dehydration and water treatment equipment and water treatment filtration system, clean water tank, recycled water tank, sludge tank and sludge oil tank according to any one of claims 1 to 15; After the oilfield produced fluid is treated with a demulsifier, it enters the oilfield produced fluid dehydration and water treatment equipment to separate gas, purified oil, produced water and sludge. The gas is transported to the natural gas processing system, the purified oil is directly transported out from the buffer chamber through the pipeline, and the produced water is stored in the clean water tank after being filtered by a single or multi-stage filter and then transported out. The backwash water obtained by the device used for backwashing the produced water enters the recovery water tank and then flows back to the enhanced oil removal chamber of the oilfield produced fluid dehydration and water treatment equipment. The oily waste collected in the enhanced oil removal chamber is stored in the oily waste tank and then returned to the oilfield produced fluid inlet of the oilfield produced fluid dehydration and water treatment equipment. The sludge separated by the oilfield produced fluid dehydration and water treatment equipment is stored in the sludge tank and transported off-site for treatment.

18. The method for dehydrating and treating oilfield produced fluid according to claim 16, characterized in that, The residence time in the density difference separation chamber is 30 min to 45 min; The residence time of the dielectric differential separation cavity is 30 min to 45 min; The residence time in the enhanced degreasing chamber is 35 min to 40 min; The residence time in the cavity for removing suspended solids is 30 to 40 minutes; The dwell time in the buffer chamber is 10 to 20 minutes; The oilfield produced fluid dehydration and water treatment equipment outputs purified oil with a water content of less than 0.5%, and the produced water separated from the produced fluid has an oil content and suspended solids content of less than 50 mg / L.

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