The way infield oil treatment and the means of its implementation
The invention relates to the field of the preparation of the products of oil wells and its division of oil, gas, and water with subsequent finishing components to marketable condition or to the demands of field use. Provides a more effective way by combining the processes of dehydration, degassing and flushing oil fresh water. The inventive method is based on the preliminary vacuumoperated flow of production wells, in which multiple microarray destroy booking the shell, there is an instant treatment phase of the emulsion, pogransloya not formed. The method is carried out in conventional and three-phase separators, including a preliminary separation of the phases and pass the components through individual nozzles. Are vacuumoperated not the emulsion, and the most resistant parts. Using a longitudinal magnetic field, flushing vacuumoperated emulsion formation and fresh water. Use an angled surface to intensify the separation of phases. Conduct end separation in three-phase separators, including additive vacuumoperated in the nozzle of gas condensate. 3 N. and 12 C.p. f-crystals, 6 ill.
2. The LEVEL of TECHNOLOGY
Infield oil preparation includes its degassing, dehydration and desalting.
The problem of oil separation is considered in a parallel application “Method of oil separation at the end of the separation units and the means for its enforcement”.
The most common nowadays thermochemical method of dehydrating oil, comprising the additive of demulsifier, friction and subsequent stratification in horizontal or inclined cylindrical apparatus (see, for example, the book Baikov N. M. and other Collection and field processing of oil, gas and water - M.: Nedra, 1981, 105 S. - prototype) due to the high cost of demulsifiers roads, requires large areas for installation of oil and metal. In addition, he has created the problem of pornsleep.
The design of the tanks is such that the dehydrated oil is collected from the upper (surface) layer and separated the water from the bottom. On the border between water and oil gradually accumulate not destroyed emulsion, the broken book obolochek is thew, sharply deteriorating the quality of its training, or exhaust water, giving rise to the problem of cleaning up to required standards.
Return caught in the water treatment process at the head of process exacerbates the problem. Reset same pornsleep in separate tanks to trap emulsions creates the problem of their disposal. Due to the high water content and pollution, however, they do not burn and can not be injected into formations, and attempts at their destruction (see, for example, EP 39001/10 - 002-89 “Technology comprehensive training trap oils and discharged water. - Ufa: Vniisptneft, 40 C.) requires individual research work and often unsuccessful.
The famous conclusion of pornsleep either end of the divider phases, either directly from the sump (for example, A. S. No. 2042375) and their individual processing (for example, in A. S. No. 1761187 - mechanical destruction, A. S. No. 1044759 - thermochemical, A. S. No. 1047491 acoustic), but to fundamentally solve the problem or not.
There is an intensive search of ways to partition a stable oil emulsions by means of:
hydraulic impact (for example, create a strongly developed turbulent flow regime when you pass the emulsion through the Laval nozzle (patent RF №2045982));
passes of the emulsion through the water SL - 500-1000 Hz, A. C. No. 1047491 - acoustic frequency, A. S. No. 700163, 749399 - high frequency field, and a dissertation Khakimov B. C. “Development of technology for the destruction of persistent oil emulsions of high-frequency electromagnetic fields in the oil fields” - Ufa, BSU, 1984) - microwave (0,15-13 MHz);
- magnetic field (A. S. No. 495040, RF patent №2095119);
- the addition of a diluent, for example, gas condensate (Petroleum engineering, 1978, No. 10, page 22-23);
- exposure electropole (see, for example, thesis of K. T. N. Shvetsov “Intensification of the process of demulsification of oil by the use of electrocoagulation with a perforated screen - Ufa, 1985, and Gershuni S. M., Labounkova M, the Equipment for dehydration and desalting of crude oil in an electric field. OI “Chemical and petroleum engineering”. M: sniti Chimneys, 1983, 33 S.)
However, to fundamentally solve the problem or not. Known methods are either too expensive or unreliable, or create new problems (e.g., in-pipe demolitia spawned streaming corrosion of pipes). Without a clear pre-define the boundaries of the effectiveness of most of the technologies in some cases effective, in others (for example, the use of pipe Velib (because the carrier salt is water) deepening oil dehydration. The efficiency of the first method is closely connected with the dispersion of the oil phase when washing. Therefore, it is not always effective and requires high consumption of fresh water. The second method involves a multi-stage dehydration and therefore bulky and expensive.
Reducing the bulkiness of the oil treatment plants can be achieved by combining different processes in one machine. So, at the stage of preliminary dehydration and separation of oils appeared three-phase separators. Until the past it was believed that the emitted gas prevents deposition of droplets of water. Cases of deep dehydration in three-phase separators showed the falsity of such representations. Thus, the LTP North orekhovskaya field (JV JSC “Sable” - Megion) three-phase separators provide quality dehydrated to a residual water content less than 0.1%, While the residual oil content in the discharged water (5-6 mg/l) is sufficient even to reset it in the sea without further purification (act test). The experience of obtaining pure water during the dehydration of oil contained in article Zaitsev Y. C. and others “the Combination of oil and water - based lsout built-in separator or remote (with discharge of trapped oil in the separator) separators.
Dehydration and desalting combined with deep dehydration of oil. Ways of combining processes of dewatering, degassing and flushing oil fresh water is not known to us.
3. THE ESSENCE OF THE INVENTION.
The processes of separation, oil dehydration and purification of produced water could be produced in a single device, if it weren't for the threat of fragmentation of drops of water in the process prior vacuumoperated. Because of this threat in the process of development of the technology of deep searchi oil on pilot stand Vniisptneft in 1989, coming to stand from oilfield pipeline selenoamino (75-80% water) oil previously obezvozhivani under pressure of 0.2-0.25 MPa. To accumulate the required amount of dehydrated oil took 2.5-3 hours. The progress of the sludge was measured by water gauge glass. But it took to evaluate the deterioration subsequent to sludge oil product tanks, and in the spring of 1990 decided on a set of oilfield water-gas mixture through destablizer (device prior vacuumoperated) thread. What was our surprise when in the water glass instead of red emulsion appeared black oil, followed by pure water. Subsequent analysis showed hasten the processing was not formed. Special experiment by pumping just typed in the usual way the emulsion from one container to another through a destablizer input with simultaneous sampling on crap at the entrance and exit showed that the efficiency of vacuumoperated is maintained throughout the range of water content: 99% (bottom layer) to 1% (the surface layer). The transition to the set emulsion with simultaneous discharge of separated water has reduced the time set dehydrated oil to 4-5 hours, and in the subsequent operation of the stand (1990-1992) set dehydrated oil was produced. The impact of vacuumoperated on the quality of the discharge water was estimated at wastewater treatment facilities in Urai (LTP of the “Urayneftegaz”. The average oil in water content is discharged from the installation of oil amounted to 6%, instant-reached 30%. And regardless of the source of the oil content, the quality of cleaning was in the range of 5-6 mg/L.
Model experiments on many DSPS Bashkortostan, Komi Republic, Perm and Tyumen regions showed that pre-vacuumoperated able to break any emulsion, but the necessary pressure to vacuumoperated different: if fresh emulsions and low-viscosity oils at atmospheric pokazalosi insufficient, and to break the old-enriched solids pogransloya on LTP in CCI “Urayneftegaz” it took the pressure of 1 MPa. If, for the purpose of oil separation at KSU enough to provide the supercritical regime, in order to secure the destruction of the emulsion need a new criterion.
Feature of the work destabilization on the oils and oil emulsions is the dependence of the detected suction (hence, the degree of supersaturation of oil by gas pressure at the entrance to the destablizer. The degree of supersaturation oil gas very strongly (exponentially) affects the intensity of nucleation. Apparently, the restriction of the inlet pressure required to fracture emulsions, due to the dimensions of the minimum water microdrops and the distance between the two newly formed nuclei. For example, the latter should not be more than the first. Then be assured destruction morniroli shells on the smallest microcaps water. The space in the oil not covered by the breaks in this period of time, under the action of surface tension forces is transferred into the ball - i.e. drop. When it is torn booking the shell moves on the surface of the formed droplets. Subsequent embryos are formed within and on the surface tension at the boundary of liquid-gas, decreasing, with the growth of the exponential. Since the surface tension at the boundary of the water-gas is approximately two times more than at the boundary between oil and gas, the intensity of the nucleation in the water millions of times less than oil. Therefore, when vacuumoperated emulsion boil the oil, not water, and the water content of the emulsion, more than at dense packing of balls (26.6 per cent) is its appeal: instead of emulsion water in oil emulsion is formed of type “oil in water”. At the same time being rich micropezidae gas droplets of oil had passed on to them by the boundary layer quickly emerge. In the absence of bottom drain due to the accumulation of any water volume that enters the emulsion after vacuumoperated, filled with water, contributing to the treatment phase.
When this saturated gas bubbles, had passed on to them booking shells, droplets of oil quickly emerge, and pogransloya not formed.
For the model experiment with bottom intake vacuumoperated samples in a limited amount (in static formation of the surface layer) is characterized by two results:
the residual water content formed of a layer of oil or less than 2%, or corresponds to a dense packing Chladni. He suggests that even after a 12-hour sludge pogransloya not go into the water phase.
The hypothesis allows to explain all the available experimental facts, but difficult to develop reliable mathematical models, which are being.
The diversity of conditions determines the ambiguity of possible solutions. Hence the multiple claims.
The way infield oil treatment involves feeding the original oil mixture in a three-phase separator may - terminal divider phase - KDF, remove products division. According to the invention is supplied either in the cage or in the KDF emulsion is passed through the device prior vacuumoperated flow - destablizer in the form of Venturi tubes with a long neck in the mode:
where R1and P2- the pressure at the entrance to the destablizer and exit;
P1-2loss of pressure on Depository when working in berasrama mode;
Ps1saturated pressure oil gas Chemie, for example, experimentally.
This method is suitable when problems pop-up coalescence of droplets not. In particular, it is applicable to deepen and accelerate the dehydration of existing facilities during their renovation.
The efficiency of the method can be significantly enhanced if the exhaust phase of the KDF to impose additional conditions.
To provide a preliminary separation of raw gas-liquid mixture in the limit divider phases and their separate input device(s). While the gas phase before entering the apparatus is passed through an adjustable nozzle of Laval, the water phase through destablizer semilattices cleaning and the oil phase through destablizer working in the above mode. Pass the gas through a Laval nozzle guarantees vacuumoperated accidentally captured oil, the passage of water through the destablizer deepens its clearance from the microdroplets of oil. Because the conditions necessary for emulsion breaking the most hard working of the other nozzles is provided with a reserve.
vacuumoperated in the specified mode is subjected to an emulsion, and its most stable part, select either KDF or from three-phase separator near the phase boundary, and then Nadson in the apparatus, either through a discharge chamber for the implementation of any actions, encouraging separation of phases;
on an area of intense deceleration of the flow in the party in destabilizing superimposed longitudinal - line current - magnetic field.
Inhibition of stream reaches hundreds of g (where g is the acceleration of gravity). When droplets of water are exempt from booking shells, like the passengers in a dramatically slowed the bus, will be confronted. The efficiency of collision polar water droplets it is possible to multiply, by arranging the location of the charges of the droplets along the current lines. Then in addition to the inertial approximation is added to the force of electrical attraction of different charges. The method of magnetic and electromagnetic processing of emulsions are known. But in the known methods, the magnetic lines of force perpendicular to the flow. Here it is assumed coincidence of magnetic field lines with the line current, for example, through the winding of the party in destabilizing non-magnetic steel. Differences in the location of the magnetic field.
Now consider the problem of coalescence of droplets of oil at high water contents of the original emulsion. It is known that turbulence enhances the coalescence of droplets, but at the same time, the measures of drops of oil. The efficiency of coalescence depends on the concentration of droplets. Hence the need to collect droplets, and then to pretransitional limited in the turbulent regime. Such a method and device for its implementation there is a pipe inclined separator, only here, unlike the prototype oil emulsion destroyed by vacuumrobotic; and other purpose - not the selection of water, and collection and coalescence vacuumoperated droplets of oil. Here vacuumoperated emulsion before admission to the surface of the final separation is passed through a layer of distilled water reservoir upward along the inclined surface.
Pre-washed in formation water emulsion is passed through a layer of fresh hot water.
When lifting along the inclined surface of the oil component, initially having a foam structure cholesterol, forming shells of gas. So the unit load gas per unit surface area at the exit of the foam structure on the surface above the permissible drop-ablation. These drops should face down. Best apleasure are formed at the turbulent motion of the gas above the surface. It also requires the optimization of conditions deptnum thread. Therefore, pre-washed emulsion is additionally subjected to thin-layer dynamic defending when runoff to the surface of the final section on the inclined tray in the mode of free-flow traffic with surface turbulent tail gas stream, while the treated gas completely or partially introduced above the surface of the downturn in the formation gravity flow.
All of the above techniques are accompanied by deep degassing of oil. Therefore, in the case when the gravity of the selection of oil and water resolved (for example, when lifting 3-hasnah separators at a sufficient height, or in the collection of commercial oil and purified water in downstream horizontal capacity, it becomes possible to ensure the preparation of oil and water in the same apparatus, including its degassing normalized to the saturated vapor pressure.
The final separation of the phases is carried out under a pressure of 0.005 MPa.
The solution has a drawback: reduced pressure separation to atmospheric involved the loss of the oil portion of the propane-butane fractions, strongly affecting the viscosity of the oil and, consequently, its dehydration. This disadvantage can be eliminated in a known manner dilution is LSI. Petroleum engineering, No. 10, 8, 1978, S. 22-23). Fear is all the more justified that the method of oil separation with advanced vacuumrobotic on the results of the acceptance test doubles the amount of selected gas while increasing its density by about 10% - i.e., an in-depth selection comes at the expense of deeper extract gases propane inclusive. The addition of condensate to the input of the party in destabilizing reduce the allowable discharge and may worsen the destruction of the emulsion when vacuumoperated. Additive in vacuumoperated mixture involves implementing a risk of increased oil saturation pressure of the gas above the permissible limit is known that gas condensate contains a lot of dissolved gases lighter than propane. The situation can be changed when applying the emulsion of gas condensate. Thus, before mixing with vacuumoperated emulsion gas condensate is subjected to pre-vacuumoperated individual party in destabilizing and introduced into the flow vacuumoperated emulsion in the form of a gas-liquid mixture.
These techniques not only reduce the viscosity of oil-water emulsions, but will adjust gazouli towards deeper extraction of light gas components (see, for example, And the research Institute. When you start technology condensate may be low. In the following will be its accumulation in the recycling process propane-butane fractions to stabilize the quantity on some individual for each oil level (up to 5-6% of the volume of oil. NC, 1990, No. 8), which is sufficient to reduce the viscosity dozens of times. The high content of condensate will in many cases reduce the temperature required heating oil or even completely suppress the furnace, at least in the warmer months, and the elimination of hydraulic losses in furnaces will create the required reserve pressure for vacuumoperated.
Close the question about the means of mixing vacuumoperated emulsion with condensate. The fact that vacuumoperated oil is a structure that is saturated with gas bubbles. When excessive turbulence, for example, when vacuumoperated sample in a closed volume impinging jet is a thousand times the pollution of water by oil in comparison with bottom entry, i.e., droplets of oil lose gas and emerge very slowly. We need to separate the water clean. Therefore, to introduce additives (condensate, produced or fresh water, including heated) best directly in disem along the inclined surface all mix quite well. Hence destablizer, perhaps with the chamber and adjusting the node representing the nozzle with a convergent tube having a cone angle of 60 to 120° and is coupled radius R=0,2 Dr with a cylindrical neck diameter, Dr, of length L=(1.5 to 2.5)Dr and a diffuser with an effective opening angle, smoothly or gradually changing from 6-10° to 15° to 20 ° and outlet diameter, providing a speed of not more than 1 m/s According to the invention in the field of speed of 3-5 m/s in the diffuser built streamlined cross with Central also streamlined body, inside are channels for feed additives at a speed of not more than 5-7 m/s associated to the flow direction, and outside there is either an annular chamber with openings for the supply of additives or feed holes surrounding the diffuser outside water when flush mounting the latter.
The ring, the camera will not need when filing as an additive settled reservoir fluid when flush mounting of the diffuser. Such a need may arise when washing paleobotany emulsions. At a flow rate of the emulsion at the point of feed additives 3-5 m/s due to the further transition of kinetic energy in potential is created sufficient to supply the head and the mi oil. The speed limit input additives caused by the same reasons.
Washing the emulsion along the inclined surface can be arranged inside a three-phase separator. Hence the oil treatment unit, including a preliminary selection of gas, possibly, furnace heating the emulsion, three phase separator, separated nefteperegonnoj by a partition into two compartments - settling and oil discharge, end separation installation and water purifiers. According to the invention a three-phase separator is equipped party in destabilizing at the entrance of the emulsion in the apparatus, the inlet migrated to the lower generatrix of the vessel at a distance of 0.5-1 m from the wall, above the entrance of the emulsion in the apparatus at a height of 0.5-1 m is welded to the lower end of the partition and the walls of the container chute, turned bottom up, open side down, the lower end of which is welded to the oil discharge septum and - perhaps - to the walls of the container, the upper end of the chute at the top does not reach the elliptic bottom of the vessel at a distance of 0.5 to 1 m in height, 0.1-0.2 m above the height of the upper edge of the oil discharge partitions for foamy oil or no higher for non-foamed PUR, meteorlogy compartment of the three-phase separator in the upper part of sabuhoro, and upper - level no higher than half of the slit, and the second row is offset from the first by 0.3 to 0.5 step, has the shape of a segment with the bottom forming at least half of the slit; and when the end of the separation in three-phase separator oil discharge compartment provided with a spatial step tray, and the existing treatment facilities for cleaning of discharged oil from the three-phase separator water can transfer mode buffer or reserve.
Explain the limitations of the claims. The location of the entrance to the separator and the lower end of the chute should exclude output emulsion outside of tray: on this plot is the output of the dehydrated oil, and such withdrawal may cause disruption of the quality of the oil. Therefore, the input area well insulated, the lower end of the chute is welded. When this circulation that occurs when you enter emulsion, podsushivaet water from the bottom of the tank, blocking the possibility of breaking notsoeasy water.
Restrictions on the exit of gas and oil from the groove due to the following reasons. The output of the gas shells creates a perturbation on the boundary surface between oil and gas. They are useful for dehydration of crude oil. But estrellada to the bottom of the tank, and will drive the foam on the wall, contributing to its destruction.
Enter the upper walls in the settling zone of the multi-functional separator. First of all, this is a barrier for foam and a prerequisite for its destruction by the gas flow. Secondly, oil is forced slightly to get under partitions, and creates the effect of periodic shake-up, which is very useful for dehydration of crude oil. And, finally, the gas is forced to change direction with the creation of vortex fields and the value of the speed due to the difference of the squares of the partitions. This contributes to the deposition of suspended in a stream of small droplets of oil. Captured by minogasanai drops of oil, occupying the lower part of the gas flow will be deposited on the wall with a sharp gas lift up. Restrictions altitude location of the edges of the plates prevents the flow of gas without turns (in a straight line).
Finally, changes in spill bays. In the existing three-phase separators settled oil, chuckling over the edge of the septum, falls on the free surface of oil, trapping the gas. Upon further release of oil into the endnote separator nothing wrong with that, most likely, the presence of gas bubbles even useful. But commercial oil having loose the second discharge oil on the free surface to perform Bezhanishvili discharge oil at the free surface is difficult to perform, in particular, when the inevitable fluctuations of the level. The change of direction of flow in the proposed embodiment, when the flow of oil from the longitudinal tray transverse reduces the speed, and hence Gazizova and two-story descent of oil reduces the length of the tray, a counter-bias transverse trays facilitates the arrangement and operation of the level sensor, the control discharge.
The three-phase separator has a drawback - the inability to control the dynamic sludge water by changing the angle of the surface because of the more important conditions of entering the inclined section and output from it. In addition, combine oil dehydration and washing with fresh water in the same apparatus capacitive almost impossible, but in dynamic conditions, when the rate of diffusive mixing is less than the speed of water supplied. Exactly the same as with dissolved salts, it is with the temperature. But before feeding hot water to bring more saline formation water. Therefore, the removal of produced water must be performed in a countercurrent to rising oil as it is produced in the pipe inclined separators when the preliminary discharge. So three is in the pre-discharge, only instead of the plot of the descent of gas and oil, generating pressure fluctuations due to the formation of shells of gas, there will be the entrance into the tank. The need for partial dehydration of oil before mixing with fresh warm water requires organization associated drainage discharged produced water. This raises the problem of where to take: for reinjection required section tootsee significant amount, i.e. an increase in the length of prelimary that can multiply to increase the area under the whole installation; supply it for aftertreatment in a three-phase separator is required to lift the end of the slope above the oil level in the separator to compensate for the reduction of weight of the liquid column in the inclined part due to the presence of gas-and-oil mixture and of the area with the lighter fresh water compared to almost pure formation water on the way to a three-phase separator. The descent of oil in three-phase separator can be realized through the system of two inclined trays, as proposed in the parallel application “Method semilattices clean water reservoir and means for its implementation”.
The inclined separators with the opposite direction of the movement of water and gas phase maximum speed reverse the capture input of oil by water. It can be reduced by performing the looping around the location input by connecting its upper end to the lower generatrix inclined pipe, and the bottom is on top. For purification discharged by looping water the latter is tilted in the same direction as the separator. The capture input of oil discharged water can be further reduced by performing the input vacuumoperated emulsion through a vertical pipe, a part of the inside section of the separator, inclined at an angle of about 45° to the horizon, and jutting inside the introductory section above its axis of symmetry. While the socket end has a bevel cut parallel to the generatrix of the section.
Hence sloping plot movement input vacuumoperated emulsion made outside of the three-phase separator and is made in the form of a pipe inclined separator connected to the upper part of the separator through a system of two inclined trays, input products in the three phase separator is made in the upper part of the elliptical bottom two pipe of large diameter, and the inclined separator is made with the input section, inclined at an angle to the horizontal of about 45°, and is equipped with a loop around the input area; however, the inclined separator at the bottom of his Calvados fresh heated water.
An EXAMPLE of carrying out the INVENTION
The first claim does not impose special requirements on the apparatus required for dehydration of oil, and the described method can be realized as an input apparatus, adapted to output the separated water, and (when the residence time in the apparatus is less than 20 min) when settling the equipment is within reach for 0.5 hour (time ensuring the conservation effect). That is partially dehydrating effect vacuumoperated be maintained, if the separator is not provided for the output water will be settling tank, such as tank. The main thing in this paragraph - mode vacuumoperated.
To determine the maximum permissible pressures at inlet and exit of the party in destabilizing the identification of three values.
For a given emulsion, these values can be found experimentally by testing models of party in destabilizing. Developed a program of research, consisting of three stages:
- test the self-similarity of the mode of determination of sizeP1-2;
- verification of the adequacy of the mode locking determination of sizeP2;
- determination amendmentsThe second claim (if any KDF) allows to stabilize the pressure at the entrance to distabilizatora and fully utilise the advantages of semilattices water purification. Here an important experimental fact that for breaking emulsions require the highest inlet pressure. In this case, gas nozzle, usually works in the sound mode locking channel, ensuring the independence of the inlet pressure from fluctuations in back pressure, and at the same time exposing vacuumoperated captured oil. Discharge at the mouth of the water nozzle is generally greater than at the mouth of the nozzle to break the emulsion, and this provides a more subtle purification of produced water, and, finally, how will unload emulsion nozzle and provides the ability to change the degree of water content of the emulsion. The implementation of this method will require an optimal input components of the original flow in the apparatus. As KDF adjacent to the surface of a section of gas-oil layer oil almost dehydrated gas is best to enter in the place of formation of the free surface of the liquid for purification from suspended droplets of oil. The exception sostavlyaiete and ethane), when the terms of the preliminary dehydration when lifting the machine may require partial input gas station lift oil to increase the speed, and therefore, reducing the thickness of rising oil. And finally, vacuumoperated water is best to enter at the beginning of the segment motion of the separated water, and if this is not possible (for example, when applying the emulsion under chute inside the tank), together with vacuumoperated emulsion.
The third method, involving vacuumoperated the most resistant part of the emulsion, the implementation requires the solution of the question of intermediate processing and the insertion vacuumoperated emulsion. Here you have the following options:
- vacuumoperated emulsion is fed into the stream of incoming raw materials for dehydration, immediately before the inlet of the device;
- vacuumoperated emulsion is fed directly into the machine in the water layer (for washing) in the input area in the apparatus main body of the emulsion;
- vacuumoperated emulsion is mixed with the solvent (condensate) or warm water, washed toward the chamber above the three-phase separator in the immediate vicinity, is divided into phases, and zi are known option of filing separated oil phase in the layer of water and water - in layer of oil.
- Dehydrated in a bypass chamber oil fully or partially small doses injected into marketable oil to prevent accumulation of pornsleep or in a furnace for burning.
The choice is individual and should be made in each case on the basis of the model tests.
The technical possibility of magnetic treatment (fourth paragraph) there is no doubt. Currently, the prepared glass model of party in destabilizing and found a ring magnet, worn on the model. It is supposed to estimate the effect of magnetic field on the strength of the emulsion and its dehydration at the first opportunity. After researching the influence of a constant magnetic field is planned for the model to wind the coil and to test the influence of the intensity of different magnetic fields to dehydration. The test results will be sent to you in the course of consideration of the application.
The basis of the fifth method is the experiment conducted from 11 to 19 October 2000 on the BPS No. 89 NGDU “Ufanet” ANK “Bashneft”, which showed that vacuumoperated accelerates the dehydration of oil about 1.5 times compared with throttling, and additional rinsing accelerates dehydration in 2-3 razrezali front of the reservoir water in space in terms of the variability of the number of released water requires regulation of its flow. This self-tuning technology due to the dependence of the pressure in the drain water from the AC gas is practically eliminated. Therefore, the regulation of water drainage. But then comes the problem of source control signal. Produced water is supplied from the fresh density and temperature. But the boundaries of their section properties may not be clear due to diffusion. Moreover, due to the vortices accompanying the passage of gas shells, possible and turbulent diffusion. To ensure the availability of the area occupied by the only fresh water in these conditions it is possible, ensuring the supply of fresh water at the rate not less than the velocity of turbulent diffusion, but the outflow of fresh water in the salt creates a threat of a breakthrough after her, and oil, which is unacceptable: the oil must leave the sloping area on the substrate of fresh water. We do not know neither theoretical nor experimental solution to this problem. At the same time the problem of cleaning oil from the crystalline salt in some fields, dedicated to the salt layers, is very serious. Currently, negotiations are underway with the Institute UGA installation of three sets of sensors of density and temperature: below the place of supply of fresh water, above him, and before the flow of oil and water on the inclined tray from lifting to control water drainage.
Dynamic sucks oil from the descent of the tray was made during tests in LTP of the “Urayneftegaz” technology semilattices clean water directly discharged from the oil treatment plants. Because of the strong contamination by solids oil collected from around the region, many of booster pumping stations, prepared only with constant discharge from the tanks with water to 6% of oil daily. Instant oil in water content reached 30%. To all modes, regardless of the initial contamination after treatment the water remained clean (5-6 mg/l residual oil). Analysis of selected oil residual water contents were not conducted.
The invention proposes to use a three-phase separator as SIC. Technical problems such translation is not present, except for two issues reported before:
the problem of delivery of the separated oil and water is solved on small fields without problems by gravity discharge into the buffer capacity with subsequent pumping of them to consumers directly or through above-ground tanks. On remote neskolko increased the location of three-phase separators useful for the purposes of the preliminary preparation of the production wells to the division during the passage of the pipe separator for path separator.
The problem of deteriorating water separation due to the loss of the propane-butane fractions partially solved with the passage of the enlargement process drops when the joint motion of the gas and oil along the inclined surface.
The invention involves the flow of condensate in vacuumoperated emulsion with advanced vacuumrobotic individual party in destabilizing. The method enhances the action of the known methods for supplying condensate to improve the quality of separation (A. S. No. 1326605) and dehydration of oil (A. Zaripov, and other Ways of intensification of the process of breaking oil-water emulsions. Petroleum engineering, No. 10, 1978, S. 22-23) by increasing the content of fractions in the recycling process and by increasing the surface mass transfer with the introduction of boiling condensate.
The fact that at equilibrium the quantity of the component remaining in the oil, in proportion to the quantity of the component in the system. Artificial input propane-butane fractions increases the number of heavy gases in the system and, consequently, in the liquid phase. When the recirculation system is enriched with number of circulating components while maintaining overall balance.
Destablizer for dehydration of oil due to high gas purification, but (to reduce naradabrokering) less at least than destablizer for KSU. Because of energy losses due to vortex formation is proportional to the square of the velocity, it is highly desirable to carry out the associated input additives and mix them, preserving the saturation of gas droplets of oil without increasing the flow velocity. This requires increasing the tightness of the cross-section area of the cone crosses the Central body of the corresponding extension of the outer walls of the channel. Condition unseparated flow limits the divergence angle of the walls. Therefore, the tightness of the thread should change smoothly enough. This can be achieved by running the front part of the Central body in the form of sharp peaks and placing edges crosses at an acute angle towards the incident flow. It is known that boundary layer separation in nozzles Venturi generates oscillations and is accompanied by the formation of gas shells (see, for example, the book Pilipenko centuries Cavitation self-oscillations. - Kiev: ND, 1989, 316 C.), which is unacceptable in our case. Therefore profilirovanie the channel walls should be treated very seriously. The presence of the outer taper opens the possibility to perform cross without external welded ring Luggage.
An example of structural embodiment of the three-phase separator shown in Fig.1-3. In horizontal cylindrical vessel 1 has a conventional three-phase separators partition 2 height corresponding to the maximum bandwidth of the blank pipe. It divides the separator into two compartments - suck and drain. Settling compartment at its bottom side provided with two nozzles: spillway approximately spherical bottom and reception vacuumoperated emulsion about partitions. Over the unloading pipe is inclined open bottom of the chute 3 with the length of the whole length of the settling section. His profile is visible on the form of the arrow A. In the upper part of the settling section is two number of partitions: the top row with partitions a segment of the form 4, and bottom 5, the profile of which is visible in the sections.
The presence of oil discharge septum provides a constant level in the settling section, but threaten to zastarivaniya intermediate layer, therefore, for the control and removal of old layers includes a nozzle with a sampling valve. The nozzle communicates with the drainage capacity of a line with two valves to allow removal of land between them and join mobile naan pipe exhaust gas from the droplet separator.
If the three-phase separator in the technological chain is connected at the output of oil from KSU in naftalina compartment in addition to sensor oil level and oil discharge nozzle nothing. If the three-phase separator is used as the SIC (Fig.1 shows this option), then in addition to them to avoid capture of free gas flowing stream, it is equipped with a system of three trays: 6 longitudinal and two symmetric to each other transverse 7. Transverse trays their top edges are welded, i.e., form a spatial angle with the edge, inclined to the horizon towards the flow of oil flowing longitudinally of the tray. The slope should be completely slow down the flow and prevent the decline of oil with the outer edges of the tray. All trays in the bottom part is made with the legs of the supports between which there is a cutout for the passage of oil. Longitudinal tray bottom edge rests on the transverse trays. The cut in it is made so that the oil can flow under it. Transverse trays paws rest on the sides of the vessel. With this top paw is located in the area of the horizontal diameter of the vessel, the bottom below it. Between the legs cut a slit, guiding flowing oil to the lower part of the vessel wall, so as to free the ode of the party in destabilizing vacuumoperated emulsion is either foam, any droplets of oil-rich gas bubbles. Because the washing efficiency is directly related to the dispersion of the wash oil, to prevent escalation of droplets of oil destablizer should be placed as close as possible to the inlet pipe, preferably with the valve directly on the outlet of the tank, to allow installation and maintenance of the party in destabilizing should be raised to the appropriate value. Torch vacuumoperated emulsion, pushing a water deviates along the inclined surface, and being much easier surrounding water, pressed against her and rushes up. Caught in the water droplets of the water, naked from the book of shells, immediately merge with the surrounding water. Captured in the rise of water in the process of movement being consolidated and exhausted outside. The foam structure of the friction forces is destroyed, forming a continuous oil phase, rich krupneishimi bubbles of gas. Captured by the flow of water getting into the oil layer, is divided into large drops that quickly settle, being filtered through a layer of oil.
At the break shells of gas through the free surface of oil trapped in relatively large drops of oil, Kotora the first partition will be delayed (and when you break through the top - and the following), and destroyed by the gas flow and sprinkler in the fall of large oil droplets. Each breakthrough of the projectile will be accompanied by volnoobrazovaniye on the surface, contributing to the rapid precipitation of the remaining drops of water. When moving to the oil discharge threshold upper layer of oil will have to get under partitions, purifying and from smaller droplets, while on the surface will not be practically anhydrous oil that will spill over the threshold into the oil discharge chamber. When the overflow tray oil spreads relatively thin layer and will be free from micro bubbles of free gas. Residual impurity gas drops of oil will be removed by the droplet separator at the outlet of gas from the tank.
When testing technology semilattices clean water was contaminated with pogransloya. That's why I had to apply measures against convective capture contaminants of water to be treated. Here she was originally placed in fresh oil and contaminated it. Experience two pilot operation stand in Vniisptneft shows that despite the breakthroughs shells gas water remained visually absolutely clean after the formation of the bottom layer of 15-20 cm Experience ek is left perfectly clean (residual oil content at the level of 5-6 mg/l) at all levels of vzliva.
In an embodiment of preparation of oil with an external pipe separator and associated washing emulsion fresh water there is individual optimization of preparation of oil for a specific field. The fact that the thickness of the layer of oil and its mode of movement will depend on the slope of the section, the speed of backward movement of water from the water content of oil and its diameter, the length of the section determines the time in this mode.
Thus, section tootsee water I (see Fig.4-6) has an angle of inclination of the generatrix, excluding the capture of distilled oil with water and ensure timely removal of oil during its ascent.
Section II (introductory) due to the large angle of inclination to the horizon and high side input avoids contamination of purified water, thanks to the creation of conditions bestoweth its passage through the bottom part of the plot, and to prevent the accumulation input of oil during its evacuation.
In addition, in the back of their part of the oil flow creates a local pressure decrease, contributing to the ash and dirt entered together with baibacirava water, the input of which is somewhat lower.
Section III - section oil dehydration. As you move through this is IPAS connected with the dehydration of oil by about half, and its diameter is selected as neoprimitive process of water purification.
Section IV - section washing the emulsion with fresh water. The perfect balance for this section is half of the input of fresh water goes down and mixed with reservoir water, half arrives together with the spin-off oil in the three phase separator. This section ends by a cross member 8 is cross-cut pipes with a diameter larger than the separator. Symmetrical input at a minimum distance from him in the crossmember welded two inclined tray 9, which fades in pipelines incomplete filling, United with capacity three-phase separator. The last can be stored cross, partition and system tray besatzung descent oil, discussed in the previous paragraph. Changes the location of the nozzles settling compartment: instead of the connection of the input of raw materials placed the nozzle of purified water; enter the same products through two large diameter pipe in the upper half of the spherical bottom. Inclined to the separator part of the system is designed so that except for the section with a flat bottom turbulence does not exceed the critical from the standpoint crushing drops.
Because real is C ascending weight and produced water retains its density, the driving force of the separation process environments is much greater than that of the prototype. This determines the intensification and improvement of the quality of separation. In addition, the transition booking shells on the pop-up droplets of oil significantly reduces the probability of formation of pornsleep or at least slows down the pace of their growth. Simultaneous deepening degassing creates prerequisites for a significant reduction of the technological chain oil treatment plants.
1. The way infield oil treatment, including the filing of the original oil mixture in three phase separator or in a three-phase separator through the end divider phase - KDF, extraction separation products - oil phase, a gas phase and a water phase, wherein the supplied either in a three-phase separator or KDF emulsion or taken out of the separator or KDF emulsion or oil phase is passed through the device vacuumoperated flow - destablizer in the form of a Venturi with a long neck in mode
P2 Ps1saturated pressure oil gas inlet destablizer; P1,2- the cost pressure on the destruction of the emulsion or the oil phase. 2. The method according to p. 1, characterized in that the gas phase is passed through an adjustable nozzle of Laval, and the water phase through destablizer semilattices cleanup. 3. The method according to p. 1, characterized in that the emulsion of the KDF or three-phase separator taken near the phase boundary, then the pump is passed through destablizer. 4. The method according to p. 1, characterized in that the zone of intensive braking of the thread in the party in destabilizing impose longitudinal line current, a magnetic field. 5. The method according to p. 1, characterized in that the treated vacuum emulsion before admission to the surface of the final separation is passed through a layer of distilled water reservoir upward along the inclined surface. 6. The method according to p. 5, characterized in that the pre-washed in formation water emulsion is passed through a layer of fresh hot water. 7. The method according to p. 5 or 6, characterized in that the pre-washed emulsion is additionally subjected to dinamicas the e free-flow traffic with surface turbulent tail gas stream, when the gas is passed through an adjustable nozzle of Laval and fully or partially injected over the surface of the downturn in the formation gravity flow. 8. The method according to one of paragraphs.1-6, characterized in that the final separation of the phases is carried out under a pressure of 0.005 MPa. 9. The method according to p. 1, characterized in that the emulsion is processed by the vacuum serves gas condensate, while before mixing with the emulsion gas condensate is subjected to preliminary vacuumoperated individual party in destabilizing and enter it into the flow of the emulsion in the form of a gas-liquid mixture. 10. Destablizer, representing a nozzle with a convergent tube having a cone angle of 60 to 120and paired with a radius of R=0,2 Dr with a cylindrical neck diameter, Dr, of length L=(1.5 to 2.5)Dr, and a diffuser with an effective opening angle, smoothly or gradually changing from 6-10up to 15-20and weekends in diameter, providing a speed of not more than 1 m/s, characterized in that in the area of speed of 3-5 m/s in the diffuser built streamlined cross with Central also streamlined body, inside of which is provided with channels for feeding additives at a speed of not more than 5-7 m/s associated to the flow direction,of a rotatable fact, he has a prechamber and a regulating unit. 12. The oil treatment unit, including pre-selection of gas, three phase separator, separated nefteperegonnoj by a partition into two compartments - settling and oil discharge, end separation installation and water purifiers, characterized in that the three-phase separator is equipped party in destabilizing at the entrance of the emulsion in the apparatus, the inlet migrated to the lower generatrix of the vessel at a distance of 0.5-1 m from the wall, above the entrance of the emulsion in the apparatus at a height of 0.5-1 m is welded to the lower end of the partition and the walls of the container chute, turned bottom up, open side down, the lower end of which is welded to the oil discharge partition the upper end of the chute at the top does not reach the elliptic bottom of the vessel at a distance of 0.5-1 m in height, 0.1-0.2 m above the height of the upper edge of the oil discharge partitions or not above it, meteorlogy compartment of the three-phase separator in its upper part provided with two rows of partitions with a step of 1.5-2 m: one row with the bottom edge level with the upper edge of the oil discharge partitions, and upper - level no higher than half of the slit, and the second row is offset from pervanovo under item 12, characterized in that when the terminal separation in three-phase separator oil discharge compartment provided with a spatial step tray, and the existing treatment facilities for cleaning discharged from the phase separator of oil and water can transfer mode buffer or reserve. 14. Installation according to p. 12, characterized in that it has a furnace heating the emulsion, and the chute is welded to the lower end of the oil discharge septum and the walls of the vessel. 15. Installation according to p. 12, characterized in that the inclined section of the movement input of the emulsion is processed by vacuum, outside of the three-phase separator and is made in the form of a pipe inclined separator connected to the upper part of the separator through a system of two inclined trays, input products in the three phase separator is made in the upper part of the elliptical bottom two pipe of large diameter, and the inclined separator is made with the input section, inclined at an angle to the horizontal of approximately 45and provided with a loop around the input area, while the inclined separator in the bottom part provided with a section tootsee water with a small inclination to the horizon and in the upper - supply the
Ps1saturated pressure oil gas inlet destablizer;
P1,2- the cost pressure on the destruction of the emulsion or the oil phase.
2. The method according to p. 1, characterized in that the gas phase is passed through an adjustable nozzle of Laval, and the water phase through destablizer semilattices cleanup.
3. The method according to p. 1, characterized in that the emulsion of the KDF or three-phase separator taken near the phase boundary, then the pump is passed through destablizer.
4. The method according to p. 1, characterized in that the zone of intensive braking of the thread in the party in destabilizing impose longitudinal line current, a magnetic field.
5. The method according to p. 1, characterized in that the treated vacuum emulsion before admission to the surface of the final separation is passed through a layer of distilled water reservoir upward along the inclined surface.
6. The method according to p. 5, characterized in that the pre-washed in formation water emulsion is passed through a layer of fresh hot water.
7. The method according to p. 5 or 6, characterized in that the pre-washed emulsion is additionally subjected to dinamicas the e free-flow traffic with surface turbulent tail gas stream, when the gas is passed through an adjustable nozzle of Laval and fully or partially injected over the surface of the downturn in the formation gravity flow.
8. The method according to one of paragraphs.1-6, characterized in that the final separation of the phases is carried out under a pressure of 0.005 MPa.
9. The method according to p. 1, characterized in that the emulsion is processed by the vacuum serves gas condensate, while before mixing with the emulsion gas condensate is subjected to preliminary vacuumoperated individual party in destabilizing and enter it into the flow of the emulsion in the form of a gas-liquid mixture.
10. Destablizer, representing a nozzle with a convergent tube having a cone angle of 60 to 120and paired with a radius of R=0,2 Dr with a cylindrical neck diameter, Dr, of length L=(1.5 to 2.5)Dr, and a diffuser with an effective opening angle, smoothly or gradually changing from 6-10up to 15-20and weekends in diameter, providing a speed of not more than 1 m/s, characterized in that in the area of speed of 3-5 m/s in the diffuser built streamlined cross with Central also streamlined body, inside of which is provided with channels for feeding additives at a speed of not more than 5-7 m/s associated to the flow direction,of a rotatable fact, he has a prechamber and a regulating unit.
12. The oil treatment unit, including pre-selection of gas, three phase separator, separated nefteperegonnoj by a partition into two compartments - settling and oil discharge, end separation installation and water purifiers, characterized in that the three-phase separator is equipped party in destabilizing at the entrance of the emulsion in the apparatus, the inlet migrated to the lower generatrix of the vessel at a distance of 0.5-1 m from the wall, above the entrance of the emulsion in the apparatus at a height of 0.5-1 m is welded to the lower end of the partition and the walls of the container chute, turned bottom up, open side down, the lower end of which is welded to the oil discharge partition the upper end of the chute at the top does not reach the elliptic bottom of the vessel at a distance of 0.5-1 m in height, 0.1-0.2 m above the height of the upper edge of the oil discharge partitions or not above it, meteorlogy compartment of the three-phase separator in its upper part provided with two rows of partitions with a step of 1.5-2 m: one row with the bottom edge level with the upper edge of the oil discharge partitions, and upper - level no higher than half of the slit, and the second row is offset from pervanovo under item 12, characterized in that when the terminal separation in three-phase separator oil discharge compartment provided with a spatial step tray, and the existing treatment facilities for cleaning discharged from the phase separator of oil and water can transfer mode buffer or reserve.
14. Installation according to p. 12, characterized in that it has a furnace heating the emulsion, and the chute is welded to the lower end of the oil discharge septum and the walls of the vessel.
15. Installation according to p. 12, characterized in that the inclined section of the movement input of the emulsion is processed by vacuum, outside of the three-phase separator and is made in the form of a pipe inclined separator connected to the upper part of the separator through a system of two inclined trays, input products in the three phase separator is made in the upper part of the elliptical bottom two pipe of large diameter, and the inclined separator is made with the input section, inclined at an angle to the horizontal of approximately 45and provided with a loop around the input area, while the inclined separator in the bottom part provided with a section tootsee water with a small inclination to the horizon and in the upper - supply the
FIELD: natural gas industry.
SUBSTANCE: the invention is pertinent to the field of natural gas industry and may be used for the field preparation of products of gas condensate pools. The method provides for separation of a gas with a delivery and a low-temperature stage of separation, a phase separation of a condensate of a delivery and low-temperature stages of separation, degassing of a condensate and de-ethanization of a condensate in an evaporating rectifying column. The whole volume of a delivery stage of separation after a preliminary degassing and heating in a recuperative heat exchanger is fed into the middle part the evaporating rectifying column as a feeding. The condensate of the low-temperature stage of separation is divided into two streams. The first stream is fed into the upper part of the evaporating rectifying column as a sprinkling, the second stream is fed in the degasator. Adjustment of the technological mode and composition of products of de-ethanization depending on output and compositions of the condensate of the delivery and a low-temperature stages of separation is conducted by a change of volumes of the streams. The technical result is - maximum degree of separation of the de-ethanizated condensate at minimum losses with a dried gas.
EFFECT: the invention ensures maximum degree of separation of the de-ethanizated condensate at minimum losses with a dried gas.