EP0662997A1 - Method for stabilising crude oils at the outlet of a well, and device therefor - Google Patents
Method for stabilising crude oils at the outlet of a well, and device thereforInfo
- Publication number
- EP0662997A1 EP0662997A1 EP94923753A EP94923753A EP0662997A1 EP 0662997 A1 EP0662997 A1 EP 0662997A1 EP 94923753 A EP94923753 A EP 94923753A EP 94923753 A EP94923753 A EP 94923753A EP 0662997 A1 EP0662997 A1 EP 0662997A1
- Authority
- EP
- European Patent Office
- Prior art keywords
- crude oil
- column
- hydrocarbons
- cut
- native
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Granted
Links
- 239000010779 crude oil Substances 0.000 title claims abstract description 125
- 238000000034 method Methods 0.000 title claims abstract description 52
- 230000003019 stabilising effect Effects 0.000 title abstract 2
- 229930195733 hydrocarbon Natural products 0.000 claims abstract description 123
- 150000002430 hydrocarbons Chemical class 0.000 claims abstract description 98
- 230000006837 decompression Effects 0.000 claims abstract description 37
- 238000004821 distillation Methods 0.000 claims abstract description 34
- 238000000926 separation method Methods 0.000 claims abstract description 33
- 239000004215 Carbon black (E152) Substances 0.000 claims abstract description 12
- 239000007788 liquid Substances 0.000 claims description 50
- 238000010521 absorption reaction Methods 0.000 claims description 41
- 239000007789 gas Substances 0.000 claims description 33
- OKTJSMMVPCPJKN-UHFFFAOYSA-N Carbon Chemical compound [C] OKTJSMMVPCPJKN-UHFFFAOYSA-N 0.000 claims description 32
- -1 C 3 hydrocarbons Chemical class 0.000 claims description 25
- 238000002347 injection Methods 0.000 claims description 15
- 239000007924 injection Substances 0.000 claims description 15
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 13
- 238000001179 sorption measurement Methods 0.000 claims description 10
- 229910052799 carbon Inorganic materials 0.000 claims description 9
- 238000005520 cutting process Methods 0.000 claims description 8
- 238000003795 desorption Methods 0.000 claims description 8
- 239000000203 mixture Substances 0.000 claims description 8
- 238000007872 degassing Methods 0.000 claims description 7
- 238000002156 mixing Methods 0.000 claims description 7
- 239000003921 oil Substances 0.000 claims description 7
- 238000004064 recycling Methods 0.000 claims description 7
- 238000002336 sorption--desorption measurement Methods 0.000 claims description 7
- 238000010908 decantation Methods 0.000 claims description 4
- 238000007599 discharging Methods 0.000 claims description 4
- 239000012528 membrane Substances 0.000 claims description 4
- 230000000087 stabilizing effect Effects 0.000 claims description 4
- 238000011144 upstream manufacturing Methods 0.000 claims description 4
- 125000004432 carbon atom Chemical group C* 0.000 claims description 2
- 239000002808 molecular sieve Substances 0.000 claims description 2
- 239000003208 petroleum Substances 0.000 claims description 2
- URGAHOPLAPQHLN-UHFFFAOYSA-N sodium aluminosilicate Chemical compound [Na+].[Al+3].[O-][Si]([O-])=O.[O-][Si]([O-])=O URGAHOPLAPQHLN-UHFFFAOYSA-N 0.000 claims description 2
- 210000002268 wool Anatomy 0.000 claims description 2
- 230000002745 absorbent Effects 0.000 claims 1
- 239000002250 absorbent Substances 0.000 claims 1
- 239000012071 phase Substances 0.000 description 7
- 238000001035 drying Methods 0.000 description 6
- 238000000605 extraction Methods 0.000 description 5
- 238000010992 reflux Methods 0.000 description 5
- 230000006641 stabilisation Effects 0.000 description 5
- 238000011105 stabilization Methods 0.000 description 5
- 238000003860 storage Methods 0.000 description 4
- 238000009834 vaporization Methods 0.000 description 4
- 230000008016 vaporization Effects 0.000 description 4
- IJGRMHOSHXDMSA-UHFFFAOYSA-N Atomic nitrogen Chemical compound N#N IJGRMHOSHXDMSA-UHFFFAOYSA-N 0.000 description 2
- CURLTUGMZLYLDI-UHFFFAOYSA-N Carbon dioxide Chemical compound O=C=O CURLTUGMZLYLDI-UHFFFAOYSA-N 0.000 description 2
- 125000004429 atom Chemical group 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 239000012530 fluid Substances 0.000 description 2
- 238000011084 recovery Methods 0.000 description 2
- 230000000630 rising effect Effects 0.000 description 2
- 239000012808 vapor phase Substances 0.000 description 2
- 239000008186 active pharmaceutical agent Substances 0.000 description 1
- 239000003463 adsorbent Substances 0.000 description 1
- 229910002092 carbon dioxide Inorganic materials 0.000 description 1
- 239000001569 carbon dioxide Substances 0.000 description 1
- 238000005265 energy consumption Methods 0.000 description 1
- 238000010438 heat treatment Methods 0.000 description 1
- 239000007791 liquid phase Substances 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
- 239000000463 material Substances 0.000 description 1
- 229910052757 nitrogen Inorganic materials 0.000 description 1
- 238000012856 packing Methods 0.000 description 1
- 238000003303 reheating Methods 0.000 description 1
Classifications
-
- 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 DRILLING; MINING
- E21B—EARTH DRILLING, e.g. DEEP 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 for stabilizing crude oils at the outlet of the extraction well and the device for implementing the method.
- 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 , C5, CQ 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 , C5, CQ and C 7 .
- it is sought to maximize the production of crude oil by trying to recover the maximum of 0 3 + but by obtaining a stabilized crude oil which does not degas or very weakly.
- 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, characterized in that it comprises at least one separation step consisting in distilling under pressure the native crude oil coming from the extraction well. in at least one distillation column, in at least two sections, including a gaseous section of C- hydrocarbons
- the cut of stabilized crude oil is drawn off at the bottom of the column.
- the distillation is carried out in a conventional manner known to those skilled in the art, whether the column is lined with trays or includes packings.
- we will create a liquid reflux at the top of the column and an upward flow of vapor, against the current of the liquid reflux, at the bottom of the column.
- part of the stabilized crude oil withdrawn at the bottom of the column after vaporization of the latter is reinjected 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-
- the part of the column located below this said injection point has the function of eliminating the hydrocarbons in Cj, C 2 and part of the C 3 from the crude oil, which allows the adjustment of the vapor pressure stabilized crude oil.
- the method according to the invention will advantageously include at least one decompression step, before the separation step.
- This decompression step will consist in partially degassing said native crude oil, in essentially absorbing the hydrocarbons from C 4 to C 7 , vaporized during the degassing, in a hydrocarbon absorption liquid stable at the pressure and the temperature of the enclosure, mixing said absorption liquid loaded with C 4 to C hydrocarbons recovered with degassed crude oil, and decanting part of the reservoir water extracted from the well with said native crude oil.
- the different operations can occur simultaneously in the same enclosure or in separate enclosures.
- the crude oil is decompressed for a decompression rate corresponding to the ratio of the inlet pressure to the outlet pressure of the crude oil between 1 and 7.
- the absorption liquid is introduced against the current of the gas flow to trap the C 4 to C 7 hydrocarbons degassed during the decompression of the crude oil.
- the absorption liquid according to the invention is a hydrocarbon from the group consisting of the distillation cuts of stabilized crude oil and the stabilized crude oil itself.
- the native crude oil entering the column is distilled in at least three sections, a gaseous section of C- hydrocarbons
- the gas cut is fractionated so as to be able to create at the top of the column a liquid reflux of C 4 and C 5 hydrocarbons containing a little of C 3 hydrocarbons.
- Part of the heavy cut of hydrocarbon withdrawn is vaporized, then reinjected into the column in order to create the rising steam flow necessary for the proper functioning of the column to be distilled.
- This heavy cup, drawn at the bottom of the column is, for its almost all, advantageously recycled as an absorption liquid for the decompression step, which avoids any consumption of additional product generating additional operating costs.
- the minimum pressure inside the distillation column is chosen so as to avoid reaching a temperature below 0 ° C in column head.
- the internal pressure of the 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 comprises at least one distillation column comprising a pipe bringing the charge of crude oil to be distilled, and at least two withdrawal pipes, one for the gaseous cutting of C 4 hydrocarbons and at C 5 , containing a part of C 3 hydrocarbons at the top of the column and the other, for cutting crude oil below the point of injection of the native crude oil into the column.
- This distillation column is connected at the top of the column, to at least one selective separation circuit by the draw-off line of the gas cut and by an injection line for the 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 advantageously comprises at least one selective separator of gaseous hydrocarbons chosen from the group of separators consisting of cryogenic groups, adsorption / desorption reactors, separators with selective membranes, and at least one gas / liquid condenser .
- the invention comprises at least one adsorption / desorption reactor filled with at least one adsorbent chosen from the group consisting of active carbon, wool residues and molecular sieves.
- the circuit comprises at least two activated carbon reactors operating alternately for the continuous implementation of the gas adsorption / desorption process, as a selective gas adsorber reactor or as desorber reactor.
- a vapor current is sent to the activated carbon, which requires an additional phase of drying of the latter.
- the sum of the times of desorption of the gases and drying of the activated carbon is at most equal to the time of adsorption of these, the operations of desorption and drying of the first reactor will occur easily while the gases are adsorbed on activated carbon from the second reactor.
- the present device advantageously comprises upstream of the distillation column a partial decompression unit of native crude oil, constituted by an enclosure in the shape of an ovoid balloon comprising in its upper part an appendage comparable to a mini-column distillation of at least two theoretical plates, said enclosure comprising an inlet pipe for native crude oil, a pipe for discharging decanted water in its lower part, an outlet pipe for decompressed crude oil, added with the liquid absorption charged with C 4 ′ to C 7 hydrocarbons, a discharge line 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.
- a partial decompression unit of native crude oil constituted by an enclosure in the shape of an ovoid balloon comprising in its upper part an appendage comparable to a mini-column distillation of at least two theoretical plates, said enclosure comprising an inlet pipe for native crude oil, a pipe for discharging decanted water in its lower part, an outlet pipe
- 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 ⁇ 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 hydrocarbons from C to C 7 , and by a pipe for discharging the decompressed crude oil to a mixing / decanting enclosure comprising a inlet pipe for the absorption liquid loaded with hydrocarbons from C to C 7 , an outlet pipe for decanted water and an outlet pipe for the mixture crude oil - absorption 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
- the line for withdrawing stabilized crude oil is located at the bottom of the column.
- the distillation column is then connected at the bottom of the column, to a circuit for recycling a part of the stabilized crude oil equipped with a reboiler by the line for withdrawing the stabilized crude oil and by a line for injecting the vaporized crude oil. , located above said draw-off line.
- the distillation column comprises at least three withdrawal pipes, one for the gas cut at the head of the column, one for the crude oil stabilized in the middle part of the column, and finally one for the heavy cutting of hydrocarbons at the bottom of the column.
- the outlet pipe of said heavy cup is connected to the inlet pipe of the absorption liquid in the enclosure of the decompression unit, to recycle the heavy cut of hydrocarbons as absorption liquid.
- the distillation column is connected, at the head of the column, to a circuit for selective separation of the gaseous cut by the withdrawal and injection pipes previously described, and, at the bottom of column, to a recycling circuit comprising a reboiler by the draw-off line for said heavy cut and by an injection line situated above this draw-off point.
- the column can be connected in its middle part to a stabilized crude oil recycling circuit equipped with a reboiler by a second draw-off line located at the same level as the stabilized crude oil draw-off line, and by a line d injection of the vaporized crude oil located above this so-called second draw-off line.
- This recycle of stabilized vaporized crude oil improves the economy of the stabilization process according to the invention.
- This recycle has the effect of heating the charge of the crude oil / adsorption liquid mixture entering the column.
- the device of the invention in order to limit the energy consumption for the vaporization of the heavy cut in the reboiler of the recycle circuit, it is advantageous to replace the plates or the lining present in the part median of the column, above the point of withdrawal of stabilized crude oil, by a material and heat exchange device which has the same separation function as the plates or the lining but which also makes it possible to heat the load in the column.
- the device further comprises at least two exchangers, the first being placed on the pipe bringing the absorption liquid into the decompression chamber in order to cool it to the maximum and the second on the stabilized crude oil evacuation pipe to bring the latter to the required storage temperature.
- the method according to the invention and its device can be easily transposed by a person skilled in the art to the treatment of condensate fields which are essentially gas deposits containing hydrocarbons from Ci to C 4 . In these fields, the aim is not to stabilize fluids but to recover liquid condensates from C 4 to Ce 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
- 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 native crude oil expanded through the valve 4 and entering the balloon la through line 3, is decompressed. Under the effect of decompression, part of the C 4 to C 7 hydrocarbons is vaporized and entrained in the mini-column 1b where these hydrocarbons are separated. Part of the hydrocarbons from C 4 to C 7 thus fall back into the balloon la.
- a hydrocarbon liquid, called absorption liquid stable at the temperature and at the pressure of the enclosure l, is injected against the flow of the gas flow, near the evacuation point of non-condensable Ci and C 2 hydrocarbons, via line 6, at the head of the mini-column via line 8.
- the absorption liquid mixes with the petroleum raw and with non-decanted deposit water, the assembly being evacuated from enclosure 1 via line 7.
- the water decanted into the flask 1a is evacuated via line 5.
- 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 hydrocarbons from C-- to C5 is evacuated via line 11 then sent to a selective separation unit 13 which will make it possible to recover all the condensed hydrocarbons in C 4 and C 5 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.
- and C 2 and the rest of the non-recovered C 3 hydrocarbons are evacuated from the separation unit 13 via line 14 to be, for example, burnt with a torch.
- 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 allows better separation from light hydrocarbons in C-
- the reactor 13a corresponds to a phase of adsorption of the hydrocarbons from C-- to C5 withdrawn from the distillation column 1 via line 11, the reactor
- the reactor 13c corresponds to a phase of drying of the activated carbon by dry gaseous hydrocarbons, not previously trapped on the activated carbon, that is to say say hydrocarbons in C-
- the line 30 brings steam generated for example by a boiler, on the activated carbon of the reactor 13b via the line 30b, the valves of the lines 30a and 30b of access to the 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 the line
- the recycled dry gaseous hydrocarbons arriving in 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 ⁇ 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 chamber 31.
- the hydrocarbons from C 4 to C 7 are vaporized and entrained with the light hydrocarbons from C x to C 3 via the outlet pipe to the column separation-absorption 35 which passes through the exchanger 33a and the valve 33b.
- the C 2 to C 3 hydrocarbons are evacuated via the outlet pipe 36, the absorption liquid is introduced through the inlet pipe 48 and finally, the absorption liquid loaded with 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 line 34 of enclosure 31 and through line 39 of enclosure 38.
- the water / crude oil / absorption liquid mixture passes through a exchanger 27 to lower the temperature of the mixture before it enters column 2.
- the cut of hydrocarbon from C to C 5 is evacuated via line 11 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 and C 5 hydrocarbons are reinjected at the top of the column via the pipes 49 then 18.
- the depropanizer operating as a distillation column comprises a reboiling circuit (line 50, reboiler 50a) at the bottom of the depropanizer and a recycle circuit connected by lines 46 and 47a to the head of the depropanizer comprising an air cooler 46a.
- the stabilized crude oil is recovered at the bottom of column 2 via line 28 connected on the one hand to a reboiling circuit 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 only the hydrocarbons of interest are back in the distillation column 2 and it also makes it possible to limit the size of the unit of selective separation. Furthermore, this depropanizer 45 provides good flexibility making it possible to produce either only crude oil, or simultaneously liquefied gases and crude oil.
- the present example aims to compare the performance of the method according to the invention with that of the prior art used.
- 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 tank.
- 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 in Ci and C 2 are vaporized and evacuated towards the torch to be burned there with a flow of
- 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.
- the table below shows the recovery rates of vaporizable C 4 to C 7 hydrocarbons for the stabilization process corresponding to the prior art (A) and the stabilization process according to the invention (X).
Abstract
Description
Claims
Applications Claiming Priority (3)
Application Number | Priority Date | Filing Date | Title |
---|---|---|---|
FR9309459 | 1993-07-30 | ||
FR9309459A FR2708663B1 (en) | 1993-07-30 | 1993-07-30 | Process for stabilizing crude oils at the outlet of the extraction well and its implementation device. |
PCT/FR1994/000950 WO1995004116A1 (en) | 1993-07-30 | 1994-07-28 | Method for stabilising crude oils at the outlet of a well, and device therefor |
Publications (2)
Publication Number | Publication Date |
---|---|
EP0662997A1 true EP0662997A1 (en) | 1995-07-19 |
EP0662997B1 EP0662997B1 (en) | 1998-12-23 |
Family
ID=9449836
Family Applications (1)
Application Number | Title | Priority Date | Filing Date |
---|---|---|---|
EP94923753A Expired - Lifetime EP0662997B1 (en) | 1993-07-30 | 1994-07-28 | Method for stabilising crude oils at the outlet of a well, and device therefor |
Country Status (9)
Country | Link |
---|---|
US (1) | US5645692A (en) |
EP (1) | EP0662997B1 (en) |
AT (1) | ATE174950T1 (en) |
DE (1) | DE69415488D1 (en) |
FR (1) | FR2708663B1 (en) |
NO (1) | NO309196B1 (en) |
OA (1) | OA10141A (en) |
RU (1) | RU2135545C1 (en) |
WO (1) | WO1995004116A1 (en) |
Families Citing this family (10)
Publication number | Priority date | Publication date | Assignee | Title |
---|---|---|---|---|
BR112012004565A2 (en) | 2009-09-01 | 2019-09-24 | Ngltech Sdn Bhd | "heavy mud suppressing apparatus and crude oil stabilization assembly and process" |
US20140001097A1 (en) * | 2011-03-18 | 2014-01-02 | Ngltech Sdn. Bhd. | Process for the recovery of crude |
RU2465304C1 (en) * | 2011-08-12 | 2012-10-27 | Виктор Александрович Крюков | Method of gas-saturated oil stabilisation |
RU2553734C1 (en) * | 2014-10-07 | 2015-06-20 | Открытое акционерное общество "Татнефть" им. В.Д. Шашина | Oil treatment method |
US10287509B2 (en) | 2016-07-07 | 2019-05-14 | Hellervik Oilfield Technologies LLC | Oil conditioning unit and process |
RU2650247C1 (en) * | 2017-09-28 | 2018-04-11 | Андрей Владиславович Курочкин | System of preparation and transportation of high-viscosity oil (options) |
CA3173974A1 (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)
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 (en) * | 1991-08-08 | 1993-10-29 | Institut Francais Petrole | PROCESS FOR THE FRACTIONATION OF OIL AND GAS ON AN OIL OIL EFFLUENT. |
-
1993
- 1993-07-30 FR FR9309459A patent/FR2708663B1/en not_active Expired - Lifetime
-
1994
- 1994-07-28 WO PCT/FR1994/000950 patent/WO1995004116A1/en active IP Right Grant
- 1994-07-28 EP EP94923753A patent/EP0662997B1/en not_active Expired - Lifetime
- 1994-07-28 US US08/406,908 patent/US5645692A/en not_active Expired - Lifetime
- 1994-07-28 RU RU95108236A patent/RU2135545C1/en active
- 1994-07-28 DE DE69415488T patent/DE69415488D1/en not_active Expired - Lifetime
- 1994-07-28 AT AT94923753T patent/ATE174950T1/en not_active IP Right Cessation
-
1995
- 1995-03-28 OA OA60631A patent/OA10141A/en unknown
- 1995-03-28 NO NO951186A patent/NO309196B1/en not_active IP Right Cessation
Non-Patent Citations (1)
Title |
---|
See references of WO9504116A1 * |
Also Published As
Publication number | Publication date |
---|---|
NO951186L (en) | 1995-03-28 |
WO1995004116A1 (en) | 1995-02-09 |
FR2708663B1 (en) | 1995-10-20 |
NO951186D0 (en) | 1995-03-28 |
RU95108236A (en) | 1996-12-10 |
EP0662997B1 (en) | 1998-12-23 |
RU2135545C1 (en) | 1999-08-27 |
DE69415488D1 (en) | 1999-02-04 |
FR2708663A1 (en) | 1995-02-10 |
US5645692A (en) | 1997-07-08 |
NO309196B1 (en) | 2000-12-27 |
OA10141A (en) | 1996-12-18 |
ATE174950T1 (en) | 1999-01-15 |
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