EP1239934A1 - Dispositif et procede de separation de residus liquides dangereux - Google Patents

Dispositif et procede de separation de residus liquides dangereux

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Publication number
EP1239934A1
EP1239934A1 EP00975018A EP00975018A EP1239934A1 EP 1239934 A1 EP1239934 A1 EP 1239934A1 EP 00975018 A EP00975018 A EP 00975018A EP 00975018 A EP00975018 A EP 00975018A EP 1239934 A1 EP1239934 A1 EP 1239934A1
Authority
EP
European Patent Office
Prior art keywords
feed
vacuum tank
liquid
solids
tank
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.)
Withdrawn
Application number
EP00975018A
Other languages
German (de)
English (en)
Inventor
Harold Arne Martinsen
Current Assignee (The listed assignees may be inaccurate. Google has not performed a legal analysis and makes no representation or warranty as to the accuracy of the list.)
Marsep International KS
Tjessem Kjell
Original Assignee
Marsep International KS
Tjessem Kjell
Priority date (The priority date 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 date listed.)
Filing date
Publication date
Application filed by Marsep International KS, Tjessem Kjell filed Critical Marsep International KS
Publication of EP1239934A1 publication Critical patent/EP1239934A1/fr
Withdrawn legal-status Critical Current

Links

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
    • C10G33/00—Dewatering or demulsification of hydrocarbon oils
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/0208—Separation of non-miscible liquids by sedimentation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/04—Breaking emulsions
    • B01D17/042—Breaking emulsions by changing the temperature
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/04—Breaking emulsions
    • B01D17/044—Breaking emulsions by changing the pressure
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D17/00—Separation of liquids, not provided for elsewhere, e.g. by thermal diffusion
    • B01D17/02—Separation of non-miscible liquids
    • B01D17/04—Breaking emulsions
    • B01D17/048—Breaking emulsions by changing the state of aggregation
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/009—Heating or cooling mechanisms specially adapted for settling tanks
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/2427—The feed or discharge opening located at a distant position from the side walls
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D21/00—Separation of suspended solid particles from liquids by sedimentation
    • B01D21/24—Feed or discharge mechanisms for settling tanks
    • B01D21/2488—Feed or discharge mechanisms for settling tanks bringing about a partial recirculation of the liquid, e.g. for introducing chemical aids
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D3/00—Distillation or related exchange processes in which liquids are contacted with gaseous media, e.g. stripping
    • B01D3/10—Vacuum distillation
    • 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
    • C10G31/00—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for
    • C10G31/06—Refining of hydrocarbon oils, in the absence of hydrogen, by methods not otherwise provided for by heating, cooling, or pressure treatment
    • 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
    • C10G7/06—Vacuum distillation
    • 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
    • E21B21/00—Methods or apparatus for flushing boreholes, e.g. by use of exhaust air from motor
    • E21B21/06—Arrangements for treating drilling fluids outside the borehole
    • E21B21/068—Arrangements for treating drilling fluids outside the borehole using chemical treatment
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2221/00—Applications of separation devices
    • B01D2221/04—Separation devices for treating liquids from earth drilling, mining

Definitions

  • the present invention regards a device and method for separation of water, oil and solids from liquid oily special wastes and sohds-stabihsed emulsions
  • Examples are slopmud emulsions from drilling activities, refinery sludge and general settlement from ship's tanks, storage tanks and production vessels This constitutes a considerable share of the total amount of special wastes today
  • Emulsions are generally stabilised by
  • an adsorbed film that is mainly wetted by the continuous phase and acts as a physical barrier to prevent contact between the dispersed droplets.
  • the adsorbed film is made up of natural surfactants, chemical additives, solids, other high-molecular compounds/ polymers, as well as adsorbed ions This will give the small, dispersed droplets m the continuous medium the same elect ⁇ cal charge, and they will thus repel each other, preventing coalescence of these particles
  • Stable emulsions in the form of oil based slopmud emulsions from drilling activities consist mainly of used drilling mud mixed in with jet water and other waste/wastewater from the offshore oil activity
  • Slopmud typically contains 10 - 20 vol ° o oil, 55 - 75 vol % water and 5 - 12 vol % solids
  • Oily drilling mud may in addition contain a certain amount of special chemicals in order to impart to the mud those qualities that are required in order to allow the mud to be used for drilling
  • the solids chiefly consists of clay (modified bentomte) that has been made hydrophobic by means of quaternary ammonium compounds with a special chemical composition
  • baryte which is used as a weighting agent and to which chemicals have also been added in order to make it hydrophobic and stable du ⁇ ng drilling It also contains small amounts of drilling fines, which will be crushed cuttings
  • the content of surface-active chemicals in the drilling mud affects the wetting characte ⁇ stics of the solids, in addition to having a stabilising effect on the emulsion under the existing alkaline pH-conditions.
  • oily slopmud emulsions are treated firstly through pH conditioning, which partly alters the wetting characte ⁇ stics of the solids and thereby destabilises the emulsion
  • Oily drilling mud is normally conditioned by lowe ⁇ ng the pH value
  • the emulsion is allowed to settle in a tank This results in an oil layer at the top of the vessel, followed by a water phase m the middle, which may be extracted and treated before the water is discharged
  • the remaining emulsion at the bottom of the tank may now have a solids content of up to twice the initial content
  • a solids content of 12- 15 vol % is not unusual by such a method, when the initial solids content is 6-8 vol
  • the remaining mud phase may now be mixed with oily cuttings with a high solids content and treated thermally in a fluidised bed unit in which the water evaporates and the oil/chemicals evaporates/is cracked, so that the base oil can be recovered and the resulting solids contain only a small residual amount of hydrocarbons ( ⁇ 500 ppm )
  • Refinery sludge often consist of stable sohds-stabi zed emulsions, and are currently treated by means of a cent ⁇ fuge in order to remove as much water as possible, following conditioning with va ⁇ ous types of chemical additives
  • Refinery sludge containing crude oil contains natural surfactants in the form of resins and asphaltenes that, in combination with wax.
  • additives and solids may cont ⁇ bute to the formation of highly stable emulsions
  • the solids in the various types of refinery sludge normally amount to about 1 - 10 vol %. and may be a mixture of coke particles, rust and salt, as well as mud and silt
  • the recovered oil is normally as a resource at the refinery
  • the remaining sludge, the volume of which is reduced by up to 30-50 %, is incinerated under conditions of added energy, e g m an incinerator, so as to leave an ash residue that must be disposed of, often at considerable costs
  • EP 141 529 desc ⁇ bes the breaking up of emulsions by means of heat Heat is added to the tank by means of inclined heating rods that extend into the emulsion After the emulsion has been broken by this heat treatment, the components are separated by means of their different densities Vapour from oil fractions with a low boiling point is extracted at the top of the vessel Treated water and oil is removed from the vessel at the bottom and the top of the vessel respectively No mention is made of separation of solids NO 159 575 desc ⁇ bes a method of reducing the content of water in oil mud The oil mud in a vessel is kept at a negative pressure and a temperature that is higher than the boiling point of water at this pressure Stir ⁇ ng of the mud takes place through mud being drained from the bottom of the vessel and fed into the vessel above the surface of the liquid, where the incoming mud is sprayed against an impact plate before running down Water vapour is drawn off at the top of the vessel and liquefied through cooling
  • the aim of this invention is to reduce
  • NO 161 076 desc ⁇ bes an apparatus for collection and disintegration of viscous petroleum emulsions, in which a demulsifying agent is used to break up the emulsion
  • the novelty of this invention is reported to be a combination of a mixing device in which the demulsifying agent is mixed into the emulsion before the emulsion reaches the collecting vessel, and a negative pressure m the collecting vessel for sucking up the emulsion
  • GB 1 409 045 desc ⁇ bes a method and an apparatus for coalescence of dispersed droplets
  • the emulsion is passed through a special packing or across a baffle where the emulsion is brought into contact with two different mate ⁇ als, one with a high surface energy and one with a low surface energy
  • WO 95/10345 also describes a treatment vessel in which an emulsion is broken up by means of heat, and in which oil and water is allowed to settle before being extracted as "pure" phases
  • SU 1755861 Al also desc ⁇ bes a vessel for breaking oil/water emulsions
  • the incoming emulsion is introduced above the surface of the water in the vessel
  • the incoming emulsion is passed across an undulating dish over which is mounted bell shaped bodies with spark plugs
  • the emulsion drains from the dish into the liquid below, where oil and water is allowed to settle p ⁇ or to the "pure" phases being extracted SU 1214-135
  • A desc ⁇ bes a solution in which the emulsion is sprayed into a vessel against a screen above the surface of the liquid, in the form of ajet
  • the impact against the screen deforms the droplets of the emulsion and breaks the emulsion
  • the liquid runs down the screen that extends below the liquid surface, where oil and water is separated by sedimentation Vapour is extracted at the top of the vessel No mention is made of temperature and pressure Also, no mention is made of separation of sohds
  • US 4 938 876 desc ⁇ bes a method of separating solids-stabilised oil/water emulsions, in which method the emulsion is heated at a high pressure (7 bar) and high temperature (170 ° C) and then subjected to a rapid pressure drop (to approximately 1 bar) by passing the mass through a nozzle into a large volume vessel Du ⁇ ng this operation, water and light oil components evaporate off, and the temperature in the vessel falls to approximately 109-115 ° C Solids are separated out by means of hydrocyclones and filters, while oil and water are separated by a continuous cent ⁇ fuge Preferably, use is made of flocculants in order to ensure efficient separation of solids
  • this object is achieved by a method of separating oil, water and solids from oily feeds in the form of emulsions and muds, where the feed has first been conditioned through pH regulation m a known manner in order to destabilise it, where the feed is first heated by being passed through an externally heated pipe, the heated feed is then led into a vacuum tank partially filled with treated feed that is undergoing final treatment in the form of settling, so that a particle- ⁇ ch fraction is deposited at the bottom of the tank underneath a liquid phase with a reduced solids content, where there is a vapour pocket at the top end of the tank, and where the pressure in the vacuum tank is lower than atmosphe ⁇ c pressure, vapou ⁇ sed liquid is extracted from the vapour pocket, liquefied and treated further, the solids are allowed to settle before being removed from the bottom of the vacuum tank for further treatment, liquid is extracted from the liquid phase for further treatment
  • Heating the feed by passing it through a pipe that is heated from the outside means that all the components of the feed are brought into contact with the surface of the pipe, ensu ⁇ ng that all the components of the feed are heated to approximately the same temperature
  • static charges that may be present in some of the feed components will be discharged upon contact with the pipe surface
  • the pipe through which the feed is passed is preferably from about more than 25 m long, more preferably more than 50 m long, and most preferably more than 100 m long.
  • the feed is preferably heated to a temperature of from 60 to 120 °C, preferably from 80 to l lO °C.
  • the absolute pressure in the vacuum tank be from 0.9 to 0.1 bar, more preferably from 0.8 to 0.3 bar, and most preferably about 0.5 bar.
  • the feed is introduced at or near the top of the vacuum tank and sprayed out against the walls of the vacuum tank, above the liquid surface.
  • the feed is introduced into the vacuum tank immediately below the liquid surface.
  • the feed it is preferable that the feed be led into a region that is horizontally delimited against the remaining contents of the tank.
  • the feed is preferably subjected to vacuum conditions in the heater.
  • a device for separating oil, water and solids from an emulsion that comprises a heater comprising an externally heated pipe for heating of the emulsion; a vacuum tank with an absolute pressure of from 0.9 to 0.1 bar, which tank is partially filled with feed in the form of emulsions and/or mud being treated, and is such that there is a vapour pocket at the top of the vacuum tank; a feed line for leading heated feed from the heater into the vacuum tank; a vapour outlet for extracting vapour from the vacuum tank; a liquid outlet for extracting liquid from the vacuum tank; and a particle outlet for extracting solids and liquid from the bottom of the vacuum tank.
  • the heater preferably comp ⁇ ses a pipe that is preferably at least 25 m, more preferably at least 50 m, and most preferably at least 100 m long, and where the pipe is heated externally, preferably by surrounding hot water
  • the feed line leads to a nozzle at or near the top of the vacuum tank
  • the feed line discharges in a ho ⁇ zontally delimited region immediately below the liquid surface in the vacuum tank
  • the negative pressure in the vacuum tank is important At a negative pressure, the components of the emulsion will boil at a lower temperature than they would at atmosphe ⁇ c pressure Boiling (vapour generation) inside the droplets of the emulsion cause the droplets to burst due to the increase in vapour volume, and the emulsion is eakened/broken
  • Breaking the emulsion may cause the re-formation of static charges These new charges will inhibit further separation by the oil and water phases not becoming clean, and thus necessitating further treatment by use of a different technology
  • By initiating the weakening/breaking of the emulsion m the heater new static charges will be removed in the heater The charges are rapidly discharged through contact with steel pipe in the heater and steel walls in the vacuum tank
  • the negative pressure also appears to have a positive effect on the solids in the emulsion
  • the solid particles may contain gas pockets or m other ways associated gas This gas can reduce the apparent density of the particles, thus preventing/reducing precipitation Bv exposing the particles to heat followed by a vacuum, the gas will be released.
  • the resulting increase in density combined with the effect of a reduction in the viscosity and density of the oil, which according to Stake's Law entails less resistance to the particles settling (precipitating), may be an explanation of why extremely small and fine particles of colloidal size ( ⁇ 2 ⁇ m) settle following treatment according to the present method
  • mud such as used d ⁇ lling mud provide special challenges, as they may in addition to microparticles such as clay and drilling fines also contain va ⁇ ous other solids in the form of wool, sawdust, animal hair and other sealing compounds that are used to prevent drilling mud from leaking into the formation du ⁇ ng d ⁇ lling Due to these solids, pipes smaller than 20 mm are easily blocked by used dnllmg mud For this reason, certain reservations are normally made regarding the dimensions of pipes and o ⁇ fices for a treatment plant for oily wastes containing large amounts of fibrous mate ⁇ als Nozzles with a large pressure drop can not be used in this connection
  • FIG. 1 shows a schematic diagram of a plant according to the invention
  • Figure 2 shows a section through a vacuum tank in a plant according to the invention
  • Figure 3 shows a section through an alternative vacuum tank
  • the plant shown m Figure 1 is a typical plant for treating va ⁇ ous types of emulsions, such as used d ⁇ lling mud or refinery sludge
  • the emulsion to be separated is fed into the plant through an inlet 1 to a pump 2 From pump 2, the emulsion is pumped through a pipe 3 to a heater 4
  • the heater is a heater with a large heat transfer area, a heater comp ⁇ sing a long, preferably helical pipe with a smooth inner surface where the pipe is heated from the outside, preferably by means of water surrounding the coil
  • the heater 4 may if desired contain two or more coils connected in parallel
  • the heating temperature may vary, all according to the composition of the emulsion to be separated
  • the temperature of the emulsion exiting the heater 4 will typically be in the range from 60 to 120 °C
  • the pressure in the heater 4 is preferably below atmosphe ⁇ c pressure, so as to subject the feed to vapour distillation already at this point As a result, the feed in the form of emulsions is already more or less broken up before it enters the vacuum tank 10
  • the heated emulsion is passed through a pipe 6 via a three-way valve 7, to an upper feed line 8 or a lower feed line 9 to a vacuum tank 10
  • the vacuum tank 10 is partially filled with emulsion being treated
  • Above the surface of the emulsion is a vapour pocket 13, indicated by broken lines in the figure
  • the pressure in the vacuum tank is preferably from about 0 9 bar to 0 1 bar absolute pressure. It has proven practical in several tests to work at an absolute pressure in the region 0.8 - 0 5 bar. Lower pressures are evaluated as required.
  • the three-way valve 7 is set so as to lead the emulsion through the upper feed line 8 to the top of the vacuum tank 10, via a nozzle 11
  • the nozzle is an omnidirectional spray nozzle that sprays the incoming emulsion against a hemisphe ⁇ cal device in the upper part of the vacuum tank, causing the emulsion to run down along the walls of the tank and into the liquid phase being treated below
  • the three-way valve 7 is set so as to lead the emulsion through the lower feed line 9
  • the lower feed line enters the vacuum tank and preferably discharges immediately below the surface of the liquid in the tank, inside an essentially vertical stabilising tube 12 Inside the stabilising tube 12, the feed line 9 is approximately ho ⁇ zontal
  • the end of the feed pipe 9 is preferably cut at an angle, such that the opening faces upward in an oblique manner, as indicated in Figure 2
  • the stabilising tube 12 has a diameter that is greater than that of the feed line, typically three to ten times larger
  • the diameter of the stabilising tube 12 is m turn from about l A to '/ ⁇ o of the diameter of the vacuum tank 10
  • the boiling of the emulsion causes the temperature of the emulsion to fall below the boiling point of the mixture, so that only the freshly added liquid boils
  • the boiling in the vacuum tank is thus limited to the liquid that flows down the tank walls around the vapour pocket 13 or inside the stabilising tube
  • the gas in the gas outlet 14 is cooled and liquefied in a cooler 18
  • the cooler 18 is a cooler with a large inner surface, preferably a cooler in which the gas to be cooled is led through a helical pipe surrounded by water
  • the construction of the cooler 18 is thus the same as that of the heater 4
  • the liquid phase from the vacuum tank 10 is extracted through the liquid outlet 15 and through a cooler 19 that is preferably of the same type as cooler 18.
  • the pressure in the vacuum tank is adjusted by balancing the supply of liquid through the feed line 8, 9 with the extraction of liquid, mud and vapour through outlets 16, 15 and 14 respectively.
  • both the liquefied gas and the liquid is fed to an oil/water separator 22.
  • This oil/water separator 22 is preferably a separator of the same type as that described in Norwegian patent application no. 19984054, or possibly a modification of this.
  • oil/water separator 22 water and oil are separated into two relatively pure phases that are removed through an oil outlet 23 and a water outlet 24 respectively. Remaining particles and material heavier than water is removed through a mud outlet 25 and led to pipe 3, from where it again passes through the plant.
  • an additional settling tank may be provided between the cooler 18 and the oil/water separator 22 in order to separate oil and water. If such an additional tank is put in, it will be possible to recover oil that is pure enough to be used without going through the oil/water separator 22. However the water normally contains impurities and should normally be cleaned further in oil/water separator 22.
  • the water in water outlet 24 from oil/water separator 22 may contain particles, for example organic grease particles that are particularly difficult to separate out. In such cases it may be necessary to remove such particles from the water by other traditional techniques such as filtration etc.
  • Figures 1 and 2 may as previously mentioned be used both for emulsions containing fibres and other materials that blocks up nozzles, in addition to emulsions without such contents. If the device is to be installed in a plant that handles the same type of emulsion on a more continuous basis, such a plant may be tailored and simplified.
  • Figure 3 shows an alternative embodiment with a stabilising tube 25 that is open to the rest of the vacuum tank at the top, but not at the bottom. This device is especially adapted to feeds with a very high solids content.
  • Mud with a high dry solids content is removed by use of a pump 27, through a mud outlet 26 at the bottom of the stabilising tube 25.
  • Gas and vapour from the gas outlet 14 and the liquid outlet 15 are treated in the same manner as in the device described above. Mud and water that sinks to the bottom of the vacuum tank 10 passes on to further treatment together with the mud from mud outlet 26 if the solids content is sufficiently high, or is otherwise recycled through the plant.
  • the heat from the coolers 16, 18 is preferably used to pre-heat the feed in the form of emulsion/mud before this is fed to the heater 4.
  • gear pumps eccentric screw pumps or preferably rotary lobe pumps.
  • Oil content 22 vol. %; Water content: 72 vol. %;
  • Operating pressure in vacuum tank - 0.4 bar (i.e. 0.4 bar below atmospheric pressure).
  • Operating mode Feed introduced through the lower feed line.
  • the remainder of the oil is in the solids, which mamly consists of light bentomte particles that have been chemically modified to swell in oil instead of water.
  • a lighter phase was also observed above the heavy phase, containing 40- 50 vol. % solids. This share amounted to just over 20 litres. The rest of the dust was distributed as small particles in the water phase.

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  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Engineering & Computer Science (AREA)
  • Oil, Petroleum & Natural Gas (AREA)
  • General Chemical & Material Sciences (AREA)
  • Organic Chemistry (AREA)
  • Geology (AREA)
  • Life Sciences & Earth Sciences (AREA)
  • Mining & Mineral Resources (AREA)
  • Environmental & Geological Engineering (AREA)
  • Fluid Mechanics (AREA)
  • Mechanical Engineering (AREA)
  • General Life Sciences & Earth Sciences (AREA)
  • Geochemistry & Mineralogy (AREA)
  • Heat Treatment Of Water, Waste Water Or Sewage (AREA)
  • Removal Of Floating Material (AREA)

Abstract

On décrit un procédé qui permet de séparer de l'huile, de l'eau et des solides présents dans des charges de résidus d'hydrocarbures sous forme d'émulsions et de boues, dans lequel la charge a d'abord été conditionnée avec une régulation du pH effectuée d'une manière connue pour déstabiliser la charge, cette dernière étant au départ chauffée au moyen de son passage dans une canalisation chauffée sur sa surface extérieure. La charge chauffée est ensuite envoyée dans une cuve à dépression partiellement remplie d'une charge elle-même soumise à un traitement final prenant la forme d'une sédimentation, la partie supérieure de la cuve comprenant une poche de vapeur et la pression dans la cuve à dépression étant inférieure à la pression atmosphérique. Du liquide sous forme de vapeur est extrait de la poche à vapeur, liquéfié puis traité, alors qu'on laisse les solides se déposer avant de les évacuer du fond de la cuve à dépression pour les traiter ensuite, et le liquide est extrait de la phase liquide pour subir un traitement ultérieur. On décrit également un dispositif permettant de mettre en oeuvre le procédé selon l'invention.
EP00975018A 1999-11-10 2000-11-10 Dispositif et procede de separation de residus liquides dangereux Withdrawn EP1239934A1 (fr)

Applications Claiming Priority (3)

Application Number Priority Date Filing Date Title
NO19995497A NO310546B1 (no) 1999-11-10 1999-11-10 Fremgangsmåte og anordning for separasjon av olje, vann og faststoff fra oljeholdige föder
NO995497 1999-11-10
PCT/NO2000/000380 WO2001034266A1 (fr) 1999-11-10 2000-11-10 Dispositif et procede de separation de residus liquides dangereux

Publications (1)

Publication Number Publication Date
EP1239934A1 true EP1239934A1 (fr) 2002-09-18

Family

ID=19903961

Family Applications (1)

Application Number Title Priority Date Filing Date
EP00975018A Withdrawn EP1239934A1 (fr) 1999-11-10 2000-11-10 Dispositif et procede de separation de residus liquides dangereux

Country Status (4)

Country Link
EP (1) EP1239934A1 (fr)
AU (1) AU1312601A (fr)
NO (1) NO310546B1 (fr)
WO (1) WO2001034266A1 (fr)

Families Citing this family (3)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
FR2922464B1 (fr) * 2007-10-18 2010-06-04 Inst Francais Du Petrole Dispositif de separation d'un solide finement divise en suspension dans un liquide visqueux
NL1040982B1 (nl) * 2014-10-03 2016-10-03 Johanna Maria Van Vught Erna Putvet-zuivering.
CN112340913A (zh) * 2020-10-10 2021-02-09 青岛科技大学东营资源化研究院 一种高效危险废液减量化撬装装置及废液处理工艺

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NO995497D0 (no) 1999-11-10
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AU1312601A (en) 2001-06-06
WO2001034266A1 (fr) 2001-05-17

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