EP0662997B1 - Verfahren zur stabilisierung von rohölen beim verlassen von einer ölgewinnungsbohrung und vorrichtung zur durchführung dieses verfahrens - Google Patents

Verfahren zur stabilisierung von rohölen beim verlassen von einer ölgewinnungsbohrung und vorrichtung zur durchführung dieses verfahrens Download PDF

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Publication number
EP0662997B1
EP0662997B1 EP94923753A EP94923753A EP0662997B1 EP 0662997 B1 EP0662997 B1 EP 0662997B1 EP 94923753 A EP94923753 A EP 94923753A EP 94923753 A EP94923753 A EP 94923753A EP 0662997 B1 EP0662997 B1 EP 0662997B1
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EP
European Patent Office
Prior art keywords
crude oil
column
hydrocarbons
pipe
cut
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EP94923753A
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English (en)
French (fr)
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EP0662997A1 (de
Inventor
Jean-Paul Gourlia
Jacques Tournier Lasserve
Georges Bihn-Cirlot
Jean Vandermeersch
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Societe National Elf Aquitaine
Societe Nationale Elf Aquitaine Production SA
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Societe National Elf Aquitaine
Societe Nationale Elf Aquitaine Production SA
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    • C—CHEMISTRY; METALLURGY
    • C10—PETROLEUM, GAS OR COKE INDUSTRIES; TECHNICAL GASES CONTAINING CARBON MONOXIDE; FUELS; LUBRICANTS; PEAT
    • C10G—CRACKING HYDROCARBON OILS; PRODUCTION OF LIQUID HYDROCARBON MIXTURES, e.g. BY DESTRUCTIVE HYDROGENATION, OLIGOMERISATION, POLYMERISATION; RECOVERY OF HYDROCARBON OILS FROM OIL-SHALE, OIL-SAND, OR GASES; REFINING MIXTURES MAINLY CONSISTING OF HYDROCARBONS; REFORMING OF NAPHTHA; MINERAL WAXES
    • C10G7/00—Distillation of hydrocarbon oils
    • C10G7/02—Stabilising gasoline by removing gases by fractioning
    • E—FIXED CONSTRUCTIONS
    • E21—EARTH OR ROCK DRILLING; MINING
    • E21B—EARTH OR ROCK DRILLING; OBTAINING OIL, GAS, WATER, SOLUBLE OR MELTABLE MATERIALS OR A SLURRY OF MINERALS FROM WELLS
    • E21B43/00—Methods or apparatus for obtaining oil, gas, water, soluble or meltable materials or a slurry of minerals from wells
    • E21B43/34—Arrangements for separating materials produced by the well

Definitions

  • the present invention relates to a method of stabilization of crude oils at the well exit of extraction and the device for implementing the process.
  • the crude oil stabilization process is understood to mean the operation which consists in reducing the flow pressure of the crude oil leaving the well, generally between 10 and 100 bars at atmospheric pressure, while respecting a Reid vapor pressure of the around 0.69 bar at 38 ° C determined by API standard D323 while limiting losses to the atmosphere of light hydrocarbons, especially C 3 + hydrocarbons, that is to say made up of three to seven atoms of carbon commonly known as C 3 , C 4 , C 5 , C 6 and C 7 .
  • C 3 + hydrocarbons that is to say made up of three to seven atoms of carbon commonly known as C 3 , C 4 , C 5 , C 6 and C 7 .
  • This flash method does not allow the selective separation of C 3 hydrocarbons - from crude oil without degassing other products with higher added value.
  • the presence of C 3 - in stabilized crude oil makes it more sensitive to variations in temperature and pressure during subsequent operations, since these, C 3 - , can degas inadvertently.
  • the aim of the present invention is therefore to obtain a stabilized crude oil in which a maximum of C 4 + hydrocarbons will be recovered, that is to say the C 4 to C 7 hydrocarbons, generally not fully recovered. by techniques known to a person skilled in the art and adjusting the quantity of C 3 hydrocarbons in order to obtain the optimum Reid vapor pressure for its storage or subsequent transport.
  • the present invention therefore relates to a process for stabilizing crude oils at the outlet of the extraction well comprising a decompression step consisting of partially degassing and decanting part of the extracted reservoir water and a separation step consisting distilling said crude oil under pressure, said method being characterized in that during the decompression step, the vaporized C 4 to C 7 hydrocarbons are absorbed in an absorption liquid which is then mixed with said petroleum degassed and in that during the separation step, the said mixture is introduced into the middle part of a distillation column and distilled in at least two sections, including a gaseous section of C 1 to C 5 hydrocarbons recovered at the head of the column, and a cut of stabilized crude oil recovered below the point of injection of the native crude oil into the column.
  • Degassing, absorption, mixing operations and settling occur simultaneously in the same enclosure, or in separate enclosures, the liquid absorption being introduced against the flow of gas to trap hydrocarbons from C4 to C7 degassed during degassing by decompression of native crude oil.
  • the liquid absorption is a hydrocarbon from the group consisting of distilled cuts of stabilized crude oil and the stabilized crude oil itself and crude oil is decompressed for a decompression rate corresponding to ratio of the inlet pressure to the outlet pressure of the crude oil between 1 and 7.
  • distillation is done in a known conventional manner skilled in the art, that the column is lined with trays or includes fillings. So, we are going to create a reflux liquid at the top of the column and an upward flow of vapor, counter-current of liquid reflux, at the bottom of the column.
  • the part of the column located above the injection point of the native crude oil has the function of separating the hydrocarbons from C 1 to C 5 from the heavier hydrocarbons.
  • the part of the column located below this said injection point has the function of eliminating the C 1 , C 2 hydrocarbons and part of the C 3 from the crude oil, which allows the adjustment of the tension of stabilized crude oil vapor.
  • the native crude oil is distilled in two cuts, said cut gas at the top of the column and the crude oil cut stabilized at the bottom of the column, part of the cut stabilized crude oil being vaporized and then reinjected into bottom of column to create the rising steam flow.
  • the native crude oil entering the column is distilled in at least three cuts, a gaseous cut of C 1 to C 5 hydrocarbons drawn off at the head of the column, then a cut of stabilized crude oil drawn off in the middle part of the column and finally a heavy section of hydrocarbons, drawn off at the bottom of the column and consisting mainly of hydrocarbons having at least eight carbon atoms per molecule.
  • the gas cut is fractionated so as to be able to create a liquid reflux of C 4 and C 5 hydrocarbons containing a little C 3 hydrocarbons at the top of the column.
  • Part of the heavy cut of hydrocarbons is vaporized, then reinjected, i.e. recycled into the column to create the rising vapor flow necessary for the proper functioning of the distillation column.
  • the other part of this heavy cup, drawn at the bottom of column is advantageously recycled as a liquid absorption for the decompression stage, which avoids any consumption of additional product generating additional operating costs.
  • the minimum pressure inside the column distillation is chosen so as to avoid reaching a temperature below 0 ° C at the top of the column.
  • Pressure internal column will generally be between 4 bars and 15 bars.
  • Another object of the invention is the device implementing said method.
  • This device is characterized in that it includes a decompression unit partial native crude oil consisting of an enclosure closed with an inlet pipe at the top gas absorption liquid, and a distillation column including an oil charge line raw after decompression to be distilled, and at least two draw-off lines for gas cutting of hydrocarbons at the top of the column, and for cutting crude oil in below the crude oil injection point in the column.
  • the distillation column is connected at the head of the column, to at least one selective separation circuit by the draw-off line of the gas cut and by a line for injecting liquid hydrocarbons mainly of C 4 and C 5 , located below. the point of withdrawal of said gaseous cut in the column.
  • the selective separation circuit includes advantageously at least one selective separator of gaseous hydrocarbons chosen from the group of separators consisting of cryogenic groups, reactors adsorption / desorption, membrane separators selective, and at least one gas / liquid condenser.
  • the preferred selective separation circuit of the invention comprises at least one reactor adsorption / desorption filled with at least one adsorbent chosen from the group consisting of activated carbon, wool residues and molecular sieves.
  • the circuit comprises at least two activated carbon reactors operating alternately for the continuous implementation of the process adsorption / desorption of gases, as an adsorber reactor gas selection or as a desorber reactor.
  • a vapor stream is sent to the activated carbon, which requires an additional phase of drying thereof.
  • desorption times gas and activated carbon drying is at most equal to adsorption time of these, desorption operations and drying of the first reactor will happen easily while the gases are adsorbed on the activated carbon of the second reactor.
  • the partial decompression unit of native crude oil is constituted by an enclosure in the shape of an ovoid balloon comprising in its upper part an appendage comparable to a mini-distillation column of at least two theoretical plates, said enclosure comprising an inlet pipe for native crude oil, an outlet pipe for decanted water in its lower part, an outlet pipe for decompressed crude oil, added with absorption liquid loaded with C 4 to C 7 , a discharge pipe for light hydrocarbons, mainly C 1 and C 2 hydrocarbons, at the upper end of the appendix, and an inlet pipe for the absorption liquid.
  • the partial decompression unit for native crude oil can be replaced by a partial decompression circuit comprising a device characterized in that it comprises, upstream of the distillation column, a partial decompression circuit native crude oil constituted by a decompression chamber for native oil connected by a gas evacuation pipe to a separation-absorption column for degassed C 1 to C 7 hydrocarbons comprising a gas outlet pipe from C 1 to C 3 , an inlet pipe for the absorption liquid and an outlet pipe for the absorption liquid loaded with C 4 to C 7 hydrocarbons, and by a pipe for discharging the decompressed crude oil to a mixing / decantation enclosure comprising an inlet pipe for the absorption liquid loaded with C 4 to C 7 hydrocarbons, an outlet pipe for decanted water and an outlet pipe for the mixture angel crude oil-liquid to be distilled.
  • a partial decompression circuit native crude oil constituted by a decompression chamber for native oil connected by a gas evacuation pipe to a separation-absorption column for degassed C 1 to
  • the stabilized crude oil withdrawal line is located at the bottom of the column.
  • the distillation column is then connected at the bottom of the column, to a recycling circuit of a part of stabilized crude oil fitted with a reboiler through the crude oil withdrawal line stabilized and by a crude oil injection pipe vaporized, located above said draw-off line.
  • the distillation column comprises at least three draw-off lines, one for gas cutting in column head, one for stabilized crude oil in the middle part of the column, and finally one for the cut heavy with hydrocarbons at the bottom of the column.
  • the outlet pipe of said cut heavy is connected to the liquid inlet pipe absorption inside the decompression unit, to recycle the heavy cut of hydrocarbons as liquid absorption.
  • the distillation column is connected, at the head of column, to a selective section separation circuit gas by the withdrawal and injection lines previously described, and, at the bottom of the column, to a circuit recycle including a reboiler by the line of withdrawal of said heavy cut and by a pipe injection located above this draw point.
  • This recycles stabilized vaporized crude oil improves the economics of the stabilization process according to the invention.
  • This recycles has the effect of heating the charge of the mixture crude oil / adsorption liquid entering the column.
  • the invention in order to limit energy consumption for vaporizing the heavy cut in the reboiler of the recycling circuit, it is advantageous to replace the trays or the upholstery present in the middle part of the column, above the point of withdrawal of crude oil stabilized, by a device for exchanging material and heat which has the same separation function as trays or that the lining but which also allows reheat the charge in the column.
  • the device also comprises at least two exchangers, the first being placed on the pipe bringing the liquid absorption in the decompression chamber for the purpose of cool to the maximum and the second on the pipe of stabilized crude oil to bring this last at the required storage temperature.
  • the method according to the invention and its device will be easily transposable by a person skilled in the art to the treatment of condensate fields which are essentially gaseous deposits containing C 1 to C 4 hydrocarbons.
  • the aim is not to stabilize the fluids but to recover the liquid condensates of C 4 to C 8 hydrocarbons.
  • a hydrocarbon fraction distilling between 200 and 300 ° C., preferably gas oil will be introduced into the fluids to be distilled and recycled as adsorption liquid.
  • Figure 1 shows a first device of the invention.
  • Figure 2 shows a selective device separation circuit
  • Figure 3 shows a second device of the invention.
  • the device in FIG. 1 comprises a decompression unit 1 for the native crude oil arriving via line 3, and a distillation column 2 sized to have 10 to 30 theoretical plates, connected to unit 1 by line 7.
  • L unit 1 is a closed enclosure, constituted by a balloon surmounted by a mini-column 1b, dimensioned for at least two theoretical plates.
  • the water / crude oil / absorption liquid mixture may pass through an exchanger 27 making it possible to lower the temperature of the mixture before it enters the distillation column 2.
  • the cut of C 1 to C 5 hydrocarbons is evacuated via line 11 and then sent to a selective separation unit 13 which will make it possible to recover all of the condensed C 4 and C 5 hydrocarbons and a portion of C 3 hydrocarbons which will be directed to a buffer tank 16 via line 15, then reinjected at the top of the column via line 18 in order to create a liquid reflux therein.
  • a valve judiciously placed on the pipe 11 makes it possible to regulate the internal pressure of the distillation column 2.
  • the C 1 and C 2 hydrocarbons and the rest of the non-recovered C 3 hydrocarbons are discharged from the separation unit 13 via line 14 to be, for example, torched.
  • the stabilized crude oil is removed by the withdrawal line 9, then its temperature is lowered by passing it through the exchanger 10 to bring it back to an acceptable temperature for its storage.
  • a second withdrawal of the stabilized crude oil is done at the same level as the previous one, via line 24.
  • the oil passes through a reboiler 25 in which it partially vaporizes, before be reinjected into column 2 above its draw-off point via line 26.
  • the reinjection of partially vaporized crude oil makes it possible to obtain a better separation from light hydrocarbons in C 1 and C 2 likely to be there still trapped.
  • the heavy section of hydrocarbons is drawn off via line 12 and then directed towards reboiler 19 to be partially vaporized there.
  • the hydrocarbon vapors are reinjected into column 2 via line 20 while the thermally stable heavy cut is recovered by line 21 and recycled as absorption liquid in the mini-column 1b of enclosure 1 via exchanger 22, the pump 23 then the pipe 8.
  • This partial vaporization of said cut makes it possible to obtain a cut of stabilized crude oil, of perfectly controlled composition.
  • FIG. 2 we have a representation of a separation unit comprising three reactors 13a, 13b and 13c, filled with activated carbon, each of them corresponding to a different treatment step.
  • the reactor 13a corresponds to a phase of adsorption of the hydrocarbons from C 1 to C 5 withdrawn from the distillation column 1 via the line 11
  • the reactor 13b corresponds to a phase of vapor desorption of the hydrocarbons trapped on the coal active
  • the reactor 13c corresponds to a phase of drying the activated carbon with dry gaseous hydrocarbons, not previously trapped on the activated carbon, that is to say the C 1 and C 2 hydrocarbons.
  • line 30 brings steam generated for example by a boiler, onto the activated carbon of reactor 13b via line 30b, the valves of lines 30a and 30b for access to reactors 13a and 13b being closed.
  • the absorbed hydrocarbons are desorbed, preferably those in C 3 , then those in C 4 and finally those in C5 and are directed via line 15b in the duct 15. They pass through a condenser 34 and are then introduced in the settling tank 36 where the condensates are evacuated via line 35 to a water treatment unit.
  • the residual C 1 and C 2 hydrocarbons are sent via line 14 'to line 14 leading to the torch, and the liquid C 3 + hydrocarbons are returned via line 17 to the buffer tank 16.
  • the valves of lines 14b and 31b are closed.
  • the recycled dry gaseous hydrocarbons arriving in the reactor 13c via line 33c are evacuated via line 14c, the valves of lines 15c and 31c being closed. They are taken to line 14 to be burnt with a torch.
  • the device of FIG. 3 comprises a decompression circuit comprising a partial decompression chamber 31 connected on the one hand to the inlet pipe 3 of the native crude oil and on the other hand to a separation-absorption column 35 of the hydrocarbons of C 1 to C 7 degassed and to a mixing / decantation enclosure 38, said column 35 being itself connected to said enclosure 38, and a distillation column 2.
  • the native crude oil arriving via line 3 is expanded in the partial decompression enclosure 31.
  • the hydrocarbons from C 4 to C 7 are vaporized and entrained with the light hydrocarbons from C 1 to C 3 via the outlet pipe to the column separation-absorption 35 which passes through the exchanger 33a and the valve 33b.
  • the hydrocarbons from C 1 to C 3 are evacuated by the outlet pipe 36, the absorption liquid is introduced by the inlet pipe 48 and finally, the absorption liquid charged with the C 4 hydrocarbons to C 7 recovered is evacuated by the outlet pipe 37 connected to the inlet pipe to the mixing / decantation enclosure 38.
  • the partially decompressed crude oil in enclosure 31 is sent via line 32 to the mixing / decantation enclosure 38 where it is mixed with the absorption liquid loaded with C 4 to C 7 hydrocarbons then discharged via line 7.
  • Decanted native water is discharged through the pipe 34 of enclosure 31 and through line 39 of enclosure 38.
  • the water / oil mixture raw / absorption liquid passes through an exchanger 27 for lower the temperature of the mixture before entering the column 2.
  • the section of hydrocarbon from C 1 to C 5 is evacuated via line 11 and then sent to a selective separation unit 13 comprising a line 14 for evacuating hydrocarbons from C 1 to C 3 and a line 15 bringing back the condensed C 4 and C 5 hydrocarbons still charged with C 3 hydrocarbons towards a depropanizer 45.
  • the major part of the purified C 4 and C 5 hydrocarbons are reinjected at the top of the column via the lines 49 then 18.
  • the propeller operating as a column distilling includes a reboiling circuit (line 50, reboiler 50a) at the bottom of the propeller and a circuit recycle connected by lines 46 and 47a to the head of the depropanizer comprising an air cooler 46a.
  • Stabilized crude oil is recovered at the bottom of column 2 via line 28 connected on the one hand to a circuit reboiling via line 40, comprising a reboiler 40a.
  • Another part of the stabilized crude oil discharged from the enclosure 43 via the pipe 44 is recycled to the column 35 as absorption liquid. It can be partially loaded with C 2 to C 4 hydrocarbons coming from the depropanizer 45 via the pipe 47b.
  • the use of a depropanizer 45 is particularly advantageous because that only are back in the distillation column 2 the interesting hydrocarbons and that it also allows limit the size of the selective separation unit.
  • this depropanizer 45 provides good flexibility to produce either only crude oil or simultaneously liquefied gases and crude oil.
  • This example aims to compare performance of the method according to the invention with those of the technique previous implementation.
  • a system of at least three flash balloons is installed making it possible to decompress native crude oil, with departures of decompression vapors charged essentially gases such as nitrogen, carbon dioxide and C 1 and C 2 hydrocarbons for the first balloon, heavier hydrocarbons for the other balloons.
  • the native crude oil comes out with a pressure of 40 bars, at a temperature of around 48 ° C and a flow rate of around 350t / h (ton / hour).
  • the pressure is reduced to 27 bars, the vaporized gases are evacuated from the balloon, then led to the torch to be burned, while the decompressed crude oil is directed to a second decompression balloon.
  • the crude oil is decompressed from 27 to 6 bars; as before, the vaporized gases are sent to the torch and the decompressed crude oil is sent to a third and final balloon in which its pressure is reduced to 1.2 bar.
  • the native crude oil sent to enclosure 1 is decompressed from 40 to 27 bars, only the gaseous hydrocarbons of C 1 and C 2 are vaporized and discharged towards the torch to be burned there with a flow rate of 37 t / h.
  • the crude oil added with the absorption liquid loaded with C 3 , C 4 and C 5 hydrocarbons is discharged from the enclosure 1 at a flow rate of 382 t / h and a temperature of 48 ° C. It is cooled to 40 ° C in the exchanger 8, then is introduced into the distillation column.
  • the stabilized crude oil is collected at a temperature of 117 ° C, at atmospheric pressure and at a flow rate of 293 t / h through line 9 at the outlet of the column.
  • the Reid vapor pressure of the recycle in the middle of the column is of the order of 0.69 bar at 38 ° C and the pressure in the column is 8.5 bar.

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Claims (28)

  1. Verfahren zur Stabilisierung eines natürlichen Rohöls am Ausgang eines Bohrlochs, das eine Stufe der Entspannung, die in seiner teilweisen Entgasung und in der Abscheidung eines Teils des entfernten Schichtwassers besteht, und eine Stufe der Abtrennung umfaßt, die darin besteht, daß man das Rohöl unter Druck destilliert, dadurch gekennzeichnet, daß im Verlauf der Stufe der Entspannung die verdampften C4-C7-Kohlenwasserstoffe in einer Absorptionsflüssigkeit absorbiert werden, die dann mit dem entgasten Erdöl gemischt wird und im Laufe der Stufe der Abtrennung das Gemisch dem mittleren Teil einer Destillationskolonne zugeführt und zu wenigstens zwei Fraktionen aufdestilliert wird, deren gasförmige C1-C5-Kohlenwasserstoff-Fraktion am Kopf der Kolonne abgetrennt wird und deren stabilisierte Rohölfraktion unterhalb der Stelle abgetrennt wird, an der das natürliche Rohöl in die Kolonne eingespritzt wird.
  2. Verfahren nach Anspruch 1, dadurch gekennzeichnet, daß die Arbeitsgänge der Entgasung, Absorption, Mischung und Dekantierung gleichzeitig in ein und demselben Raum oder in getrennten Räumen durchgeführt werden.
  3. Verfahren gemäß den Ansprüchen 1 und 2, dadurch gekennzeichnet, daß man die Absorptionsflüssigkeit im Gegenstrom zum Gasstrom zuführt, um während der Entspannung des nativen Rohöls die entgasten C4-C7-Kohlenwasserstoffe abzufangen.
  4. Verfahren gemäß den Ansprüchen 1 bis 3, dadurch gekennzeichnet, daß die Absorptionsflüssigkeit ein Kohlenwasserstoff der Gruppe, bestehend aus Fraktionen der Destillation des stabilisierten Rohöls und dem stabilisierten Rohöl selbst, ist.
  5. Verfahren gemäß den Ansprüchen 1 bis 4, dadurch gekennzeichnet daß man das native Rohöl so entspannt, daß der Druck in einem dem Entspannungsgrad entsprechenden Verhältnis von 1 bis 7 verringert wird.
  6. Verfahren gemäß den Ansprüchen 1 bis 5, dadurch gekennzeichnet, daß die gasförmige Fraktion wahlweise in zwei Fraktionen aufgetrennt wird, von denen die eine aus leichten C3-Kohlenwasserstoffen und die andere aus C4- und C5-Kohlenwasserstoffen und ein Teil aus C3-Kohlenwasserstoffen besteht.
  7. Verfahren gemäß den Ansprüchen 1 bis 6, dadurch gekennzeichnet, daß nur die die C4- und C5-Kohlenwasserstoff enthaltende Fraktion abgetrennt, dann kondensiert und schließlich erneut am Kopf der Kolonne wieder eingespritzt wird.
  8. Verfahren gemäß den Ansprüchen 1 bis 7, dadurch gekennzeichnet, daß die wahlweise Abtrennung der gasförmigen Fraktion nach einer Methode durchgeführt wird, die aus der Gruppe ausgewählt wird, bestehend aus Tiefsttemperaturtechnik, Adsorption/Desorption dieser Gase und Auftrennung der Gase an einer Membran.
  9. Verfahren gemäß den Ansprüche 1 bis 8, dadurch gekennzeichnet, daß die die C3-C5-Kohlenwasserstoffe enthaltende Fraktion entpropanisiert wird.
  10. Verfahren gemäß den Ansprüchen 1 bis 9, dadurch gekennzeichnet, daß das native Rohöl zu zwei Fraktionen aufdestilliert wird, und zwar zur gasförmigen Fraktion am Kopf der Kolonne und zur stabilisierten Rohölfraktion am Boden der Kolonne, wobei ein Teil der Fraktion des stabilisierten Rohöls verdampft und dann erneut am Boden der Kolonne eingespritzt wird.
  11. Verfahren gemäß den Ansprüchen 1 bis 9, dadurch gekennzeichnet, daß das in die Destillationskolonne eintretende native Rohöl zu drei Fraktionen destilliert wird, und zwar zu einer am Kopf der Kolonne abgezogenen gasförmigen C1-C5-Kohlenwasserstoff-Fraktion, zu einer im mittleren Teil der Kolonne abgezogenen Fraktion aus stabilisiertem Rohöl und schließlich zu einer am Boden der Kolonne abgezogenen schweren Kohlenwasserstoff-Fraktion, die in der Hauptsache aus Kohlenwasserstoffen mit wenigstens 8 C-Atomen pro Molekül steht.
  12. Verfahren gemäß Anspruch 11, dadurch gekennzeichnet, daß ein Teil der schweren Fraktion als Adsorptionsflüssigkeit wieder der Entspannungsstufe zugeführt wird und der übrige Teil verdampft und dann am Boden der Kolonne wieder eingespritzt wird.
  13. Verfahren gemäß den Ansprüchen 11 und 12, dadurch gekennzeichnet, daß ein Teil der Fraktion aus stabilisiertem Rohöl verdampft und in den mittleren Teil der Kolonne oberhalb der Stelle, an der sie abgezogen wird, wieder eingespritzt wird.
  14. Verfahren gemäß den Ansprüchen 11 bis 13, dadurch gekennzeichnet, daß der Innendruck der Destillationskolonne 4 bis 15 bar beträgt.
  15. Vorrichtung zur Durchführung des Verfahrens gemäß einem der Ansprüche 1 bis 14, dadurch gekennzeichnet, daß sie eine Einheit zur teilweisen Entspannung (1) des nativen Rohöls, bestehend aus einem geschlossenen Raum, der am Kopf eine Leitung (8) für die Zufuhr einer Flüssigkeit für die Absorption der Gase und eine Destillationskolonne (2) umfaßt, die ihrerseits eine Leitung (7) für die Zufuhr der zu destillierenden Rohölcharge nach der Entspannung und wenigstens zwei Leitungen für den Abzug der gasförmigen Kohlenwasserstoff-Fraktion am Kopfe der Kolonne (11) und für die Rohöl fraktion (9) unterhalb der Stelle, an der das Rohöl in die Kolonne eingespritzt wird, umfaßt.
  16. Vorrichtung nach Anspruch 15, dadurch gekennzeichnet, daß die Kolonne am Kolonnenkopf mit wenigstens einem Kreislauf zur selektiven Abtrennung (13) über die Leitung (11) für den Abzug der gasförmigen Fraktion und über eine Leitung (18) zum Einspritzen der flüssigen Kohlenwasserstoffe, die in der Hauptsache aus C4- und C5-Kohlenwasserstoffen bestehen, die unterhalb der Stelle angeordnet ist, an der die gasförmige Fraktion aus der Kolonne abgezogen wird, verbunden ist.
  17. Vorrichtung nach Anspruch 16 bis 19, dadurch gekennzeichnet, daß der Kreislauf der selektiven Auftrennung wenigstens einen in bezug auf gasförmige Kohlenwasserstoffe selektiven Abscheider (13a oder 13b oder 13c), ausgewählt unter Tiefsttemperaturabscheidern, Adsorptions-/Desorptionsreaktoren mit selektiven Membranen arbeitenden Separatoren, und wenigstens einen Flüssiggaskondensatorkühler umfaßt.
  18. Vorrichtung nach Anspruch 17, dadurch gekennzeichnet, daß der Kreislauf der selektiven Auftrennung wenigstens einen Adsorptions-/Desorptionsreaktor (13a oder 13b oder 13c) umfaßt, der wenigstens mit einem Absorbens, ausgewählt aus der Gruppe der Aktivkohlen, Wollrückständen und Molekularsiebe ausgestattet ist.
  19. Vorrichtung nach einem der Ansprüche 17 und 18, dadurch gekennzeichnet, daß der Kreislauf der selektiven Abscheidung wenigstens zwei Aktivkohlereaktoren (13a, 13b oder 13c) umfaßt, die zur kontinuierlichen Durchführung der Phasen der Adsorption und Desorption der Kohlenwasserstoffe alternierend arbeiten.
  20. Vorrichtung nach einem der Ansprüche 16 bis 19, dadurch gekennzeichnet, daß sie unterhalb des Kreislaufs zur selektiven Abscheidung wenigstens einen Entpropaner umfaßt.
  21. Vorrichtung nach einem der Ansprüche 15 bis 20, dadurch gekennzeichnet, daß die Einheit (1) zur teilweisen Entspannung des nativen Rohöls aus einem geschlossenen Raum in Form eines eiförmigen Behälters (la), der in seinem oberen Teil ein Aufsatz (1b) umfaßt, der mit einer Minidestillationskolonne aus wenigstens zwei theoretischen Böden vergleichbar ist, besteht, wobei dieser Raum in seinem unteren Teil eine Leitung (3) für die Zufuhr des natürlichen Rohöls, eine Leitung (5) für die Ableitung des abgeschiedenen Wassers, eine Leitung (7) für den Austritt des entspannten Rohöls, dem die mit C4-C7-Kohlenwasserstoffen beladene Absorptionsflüssigkeit zugesetzt ist, am oberen Ende des Aufsatzes eine Leitung (6) für die Ableitung der leichten C1-C2-Kohlenwasserstoffe und eine Leitung (8) für die Zufuhr der Absorptionsflüssigkeit umfaßt.
  22. Vorrichtung nach einem der Ansprüche 15 bis 20, dadurch gekennzeichnet, daß die Entspannungsanlage aus einem Kreislauf für die teilweise Entspannung des nativen Rohöls besteht, der einen Raum (31) für die Entspannung des nativen Erdöls, der über eine Leitung (33) für die Ableitung der Gase mit einer Kolonne (35) für die Abscheidung/Absorption der entgasten C1-C7-Kohlenwasserstoffe, die eine Leitung (36) für den Austritt der Gase, eine Leitung (48) für die Zufuhr der Absorptionsflüssigkeit und eine Leitung (37) für den Austritt der mit C4-C7-Kohlenwasserstoffen beladenen Absorptionsflüssigkeit umfaßt, und über eine Leitung (32) zur Ableitung des entspannten Rohöls mit einen Raum (38) für die Mischung und Dekantierung verbunden ist, der eine Leitung (37) für die Zufuhr der mit C4-C7-Kohlenwasserstoffen beladenen Absorptionsflüssigkeit, eine Leitung (39) für den Austritt des dekantierten Wassers und eine Leitung (7) für den Austritt des Gemisches aus Rohöl und zu destillierender Absorptionsflüssigkeit umfaßt.
  23. Vorrichtung nach einem der Ansprüche 15 bis 22, dadurch gekennzeichnet, daß die Leitung (9) für den Abzug des stabilisierten Rohöls am Boden der Kolonne angeordnet ist.
  24. Vorrichtung nach Anspruch 23, dadurch gekennzeichnet, daß die Destillationskolonne (2) am Boden der Kolonne mit einem Kreislauf für die Rückführung eines Teils des stabilisierten Rohöls, der mit einem Erhitzer ausgestattet ist, über die Leitung (9) für den Abzug des stabilisierten Rohöls und über eine oberhalb der Abzugsleitung angeordnete Leitung (9) für die Einspritzung des verdampften Rohöls verbunden ist.
  25. Vorrichtung nach einem der Ansprüche 15 bis 22, dadurch gekennzeichnet, daß die Destillationskolonne wenigstens drei Abzugsleitungen umfaßt, und zwar eine Leitung (11) für die gasförmige Fraktion am Kopf der Kolonne, eine Leitung (9) für die Fraktion des stabilisierten Rohöls im Mittelteil der Kolonne und schließlich eine Leitung (12) für die Fraktion der schweren Kohlenwasserstoffe am Boden der Kolonne.
  26. Vorrichtung nach Anspruch 25, dadurch gekennzeichnet, daß die am Boden der Kolonne (2) angeordnete Leitung (12) für den Abzug der Fraktion der schweren Kohlenwasserstoffe einerseits mit der Leitung (8) für die Zufuhr der Absorptionsflüssigkeit zum Raum (1) der Entspannungseinheit und andererseits mit dem Kreislauf für die Rückführung eines Teils der schweren Fraktion, der einen Erhitzer (19) und eine Leitung (20) zum Einspritzen dieser Fraktion in die Kolonne (2) oberhalb der Abzugsstelle (12) umfaßt, verbunden ist.
  27. Vorrichtung nach einem der Ansprüche 25 und 26, dadurch gekennzeichnet, daß die Kolonne (2) in ihrem Mittelteil zumindest mit einem Kreislauf für die Rückführung eines Teils des stabilisierten Rohöls, der mit einem Erhitzer (25) ausgestattet ist, über eine zweite, auf demselben Niveau wie die Leitung (9) für den Abzug des stabilisierten Rohöls angeordnete Abzugsleitung (24) und über eine Leitung (26) für die Einspritzung des verdampften Rohöls oberhalb dieser zweiten Abzugsleitung (24) verbunden ist.
  28. Vorrichtung nach einem der Ansprüche 25 bis 27, dadurch gekennzeichnet, daß sie wenigstens zwei Austauscher umfaßt, von denen der erste (22) vorzugsweise in die Leitung (21), welche die Absorptionsflüssigkeit dem Raum zuführt, eingebaut ist und die zweite (10) vorzugsweise in die Leitung für die Ableitung des stabilisierten Rohöls eingebaut ist.
EP94923753A 1993-07-30 1994-07-28 Verfahren zur stabilisierung von rohölen beim verlassen von einer ölgewinnungsbohrung und vorrichtung zur durchführung dieses verfahrens Expired - Lifetime EP0662997B1 (de)

Applications Claiming Priority (3)

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FR9309459 1993-07-30
FR9309459A FR2708663B1 (fr) 1993-07-30 1993-07-30 Procédé de stabilisation des pétroles bruts à la sortie du puits d'extraction et son dispositif de mise en Óoeuvre.
PCT/FR1994/000950 WO1995004116A1 (fr) 1993-07-30 1994-07-28 Procede de stabilisation des petroles bruts a la sortie du puits d'extraction et son dispositif de mise en ×uvre

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EP0662997A1 EP0662997A1 (de) 1995-07-19
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WO2011028093A1 (en) * 2009-09-01 2011-03-10 Ngltech Sdn. Bhd. Slug suppressor apparatus and crude oil stabilization assembly and process therefor
BR112013023909A2 (pt) * 2011-03-18 2019-09-24 Ngl Tech Sdn Bhd processo para recuperação de petróleo bruto
RU2465304C1 (ru) * 2011-08-12 2012-10-27 Виктор Александрович Крюков Способ стабилизации газонасыщенной нефти
RU2553734C1 (ru) * 2014-10-07 2015-06-20 Открытое акционерное общество "Татнефть" им. В.Д. Шашина Способ подготовки нефти
US10287509B2 (en) 2016-07-07 2019-05-14 Hellervik Oilfield Technologies LLC Oil conditioning unit and process
RU2650247C1 (ru) * 2017-09-28 2018-04-11 Андрей Владиславович Курочкин Система подготовки и транспортировки высоковязкой нефти (варианты)
WO2022170252A1 (en) * 2021-02-08 2022-08-11 Pioneer Energy, Inc System and method for oil production equipment that minimizes total emissions
US11725152B2 (en) 2021-06-02 2023-08-15 Maze Environmental Llc System and method of reducing emissions and increasing swell in an oil conditioning process
US20230347263A1 (en) * 2022-04-28 2023-11-02 Bell Engineering, Inc. Oil Vacuum Stabilizer
US11878260B1 (en) 2022-07-30 2024-01-23 Chevron U.S.A. Inc. Three phase separation in a distillation column

Family Cites Families (8)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
GB728234A (en) * 1951-08-25 1955-04-13 Lummus Co Improvements in or relating to petroleum distillation
US3091586A (en) * 1959-12-15 1963-05-28 Exxon Research Engineering Co Hydrofining of shale oil
US3320159A (en) * 1964-06-08 1967-05-16 Phillips Petroleum Co Controlling reflux in a distillation process
US3297566A (en) * 1964-10-01 1967-01-10 Phillips Petroleum Co Gas oil reflux controller
US3819511A (en) * 1973-03-12 1974-06-25 Mobil Oil Corp Distilling a crude oil
US4406743A (en) * 1981-06-15 1983-09-27 Phillips Petroleum Company Fractionation column for reclaiming used lubricating oil
US4673490A (en) * 1985-08-23 1987-06-16 Fluor Corporation Process for separating crude oil components
FR2680200B1 (fr) * 1991-08-08 1993-10-29 Institut Francais Petrole Procede de fractionnement d'huile et de gaz sur un effluent de gisement petrolier.

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ATE174950T1 (de) 1999-01-15
DE69415488D1 (de) 1999-02-04
RU2135545C1 (ru) 1999-08-27
FR2708663B1 (fr) 1995-10-20
NO951186D0 (no) 1995-03-28
OA10141A (fr) 1996-12-18
NO309196B1 (no) 2000-12-27
WO1995004116A1 (fr) 1995-02-09
NO951186L (no) 1995-03-28
EP0662997A1 (de) 1995-07-19
FR2708663A1 (fr) 1995-02-10
RU95108236A (ru) 1996-12-10
US5645692A (en) 1997-07-08

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