WO2006048299A1 - Continuous porous bed centrifuge - Google Patents

Continuous porous bed centrifuge Download PDF

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Publication number
WO2006048299A1
WO2006048299A1 PCT/EP2005/011807 EP2005011807W WO2006048299A1 WO 2006048299 A1 WO2006048299 A1 WO 2006048299A1 EP 2005011807 W EP2005011807 W EP 2005011807W WO 2006048299 A1 WO2006048299 A1 WO 2006048299A1
Authority
WO
WIPO (PCT)
Prior art keywords
centrifuge
particles
filling
centrifuge according
outer skirt
Prior art date
Application number
PCT/EP2005/011807
Other languages
French (fr)
Inventor
Martin Bartosek
Simona Biagi
Original Assignee
Eni S.P.A.
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
Priority to AT05800671T priority Critical patent/ATE518597T1/en
Application filed by Eni S.P.A. filed Critical Eni S.P.A.
Priority to MX2007005539A priority patent/MX2007005539A/en
Priority to AU2005300696A priority patent/AU2005300696B2/en
Priority to BRPI0517447-3A priority patent/BRPI0517447A/en
Priority to EA200700612A priority patent/EA010536B1/en
Priority to EP05800671A priority patent/EP1809423B1/en
Priority to US11/577,992 priority patent/US7708681B2/en
Priority to PL05800671T priority patent/PL1809423T3/en
Priority to DK05800671.9T priority patent/DK1809423T3/en
Priority to CA2581416A priority patent/CA2581416C/en
Publication of WO2006048299A1 publication Critical patent/WO2006048299A1/en
Priority to NO20072143A priority patent/NO20072143L/en
Priority to EGNA2007000416 priority patent/EG24700A/en

Links

Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B04B1/02—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles without inserted separating walls
    • 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
    • B01D17/0202—Separation of non-miscible liquids by ab- or adsorption
    • 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
    • B01D17/0217—Separation of non-miscible liquids by centrifugal force
    • 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
    • B01D17/045—Breaking emulsions with coalescers
    • 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
    • B01D17/08—Thickening liquid suspensions by filtration
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B04B1/04—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with inserted separating walls
    • B04B1/08—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with inserted separating walls of conical shape
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B1/00—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles
    • B04B1/10—Centrifuges with rotary bowls provided with solid jackets for separating predominantly liquid mixtures with or without solid particles with discharging outlets in the plane of the maximum diameter of the bowl
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B04—CENTRIFUGAL APPARATUS OR MACHINES FOR CARRYING-OUT PHYSICAL OR CHEMICAL PROCESSES
    • B04B—CENTRIFUGES
    • B04B7/00—Elements of centrifuges
    • B04B7/08—Rotary bowls
    • B04B7/12—Inserts, e.g. armouring plates
    • B04B7/16—Sieves or filters
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10—TECHNICAL SUBJECTS COVERED BY FORMER USPC
    • Y10S—TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y10S494/00—Imperforate bowl: centrifugal separators
    • Y10S494/901—Imperforate bowl: centrifugal separators involving mixture containing oil

Definitions

  • the present invention relates to a continuous porous bed centrifuge. More specifically, the present invention relates to a continuous porous bed centrifuge for the continuous separa ⁇ tion of immiscible liquids, for example water and mineral oil/petroleum, obtained by a modification to conventional disk centrifuges for increasing their efficiency.
  • the disks have been substituted by a filling of solid particles which act as a filtrating and coalescent bed. Tests have been successfully carried out for deoiling of water associated with oil production.
  • Disk centrifuges are apparatuses used for the continu- ous or semi-continuous separation of liquids, possibly con ⁇ taining solid particles, baked on the action of centrifugal force on the fluid introduced into a rotor.
  • centrifuges are considered which allow the discharge of the heavy liquid phase (aqueous) .
  • the inner part of rotors of conventional centrifuges generally contains truncated cone-shaped disks with spacers and holes for conveying the liquids.
  • the heavy phase (liquid or solid) is concentrated in the outer part whereas the light phase tends to rise towards the rotation axis.
  • the discharges of the two liquid phases leave the ro ⁇ tor and are collected by specific channels situated on the outer container.
  • the discharge of the heavy liquid phase is controlled by a kind of weir (generally a disk with an in ⁇ ternal calibrated hole) depending on to the fluid and oper ⁇ ating conditions.
  • the solids which accumulate in the rotor can be discharged at pre-established intervals.
  • the com- plete discharge of the rotor is controlled by a washer ac ⁇ tivated by a hydraulic circuit which exploits the thrust generated by the centrifugal force.
  • the Applicants have now found that it is possible to provide various improvements to the purification process of layer water (heavy phase) which substantially reduces the concentrations of oil in waste water. It has been found, in fact, that it is possible to modify a conventional disk centrifuge by eliminating the disks and adapting the system so as to enable a filtrating filling to be charged and dis ⁇ charged during the rotation of the centrifuge.
  • the modifi ⁇ cation introduced is aimed at forming a filtrating and coa- lescent bed subjected to centrifugal force in order to fa ⁇ vour the adhesion of the oil particles to the porous sur- face of the bed and separate them from the aqueous phase.
  • An object of the present invention therefore relates to a continuous porous bed centrifuge for the continuous separation of a fluid consisting of two immiscible liquids in dispersion, which comprises: a) a first outer compact essentially conical-shaped rotat ⁇ ing skirt; b) a second inner compact essentially conical-shaped skirt, integral with the outer skirt and positioned so as to form an interspace with said outer skirt; c) a perforated toroidal-shaped separation element posi ⁇ tioned at the base of the two skirts and suitable for separating the interspace from the inside of the centri ⁇ fuge; d) a closing base integral with the outer skirt by means of a sealing gasket;
  • a section equipped with a weir acting as a flow regula ⁇ tor, fixed at the head of the outer skirt and with open ⁇ ings for the discharge of the separated liquids; f) a first coaxial tube, integral with the outer skirt and with section (e) ; g) a second coaxial tube which is not integral with the outer skirt, positioned inside the first tube, for the feeding of the dispersion; h) a filling in the form of particles capable of filling from 40 to 70% of the inner volume of the centrifuge.
  • the particle fill ⁇ ing is contained inside the rotating system and is kept separate from the interspace between the two skirts by means of the toroidal-shaped separation element which has a width which is substantially identical to the thickness of the interspace.
  • the separation element can be a net, a small-holed grid or a septum with calibrated holes or pores in relation to the dimension of the particles of the fill ⁇ ing to be retained.
  • the separation element is positioned in the area which is as far away as possible from the rotation axis so as to catch the heavier liquid (for example deoiled water) .
  • the fed fluid is forced outwards by the centrifugal force and passes through the bed of particles and is filtered.
  • the heavy phase con- sequently flows through the separation element (net) , passes into the cavity between the outer skirt and inner skirt and is discharged outside.
  • cen ⁇ trifugal force the filtering particles are withheld by the separation element.
  • the filtering and coalescent bed preferably consists of particles, for example sand, or spheres having different particle-sizes.
  • the surfaces of the particles of the filling can be treated so as to have specific surface tension characteristics.
  • the filling particles are spherical to favour their charging and discharging but can have any other shape, for example the form of cylinders, cubes, or other geometrical forms, balls of microfibers or generic sand.
  • the particles can be full or with cavities and the surfaces can be smooth or porous to increase the coales ⁇ cence effect .
  • the density of the solid particles must be greater than that of the light liquid phase. It is preferable but not compulsory for them to be even denser than the heavy liquid phase.
  • the particles are rigid and can be treated on the sur ⁇ face to change the wettability and favour the coalescence process and facilitate the detachment between the grains both in the discharging and charging phase.
  • Silicone coat ⁇ ings and treatment with silanizing agents have been tested on silicate small spheres.
  • the particles can be made of glass, polymeric materi- als, metal, oxides (for example silica, silicates, alu ⁇ mina), ion exchange resins, zeolites, hollow glass micro ⁇ spheres, sands, diatomaceous earth, but also crystals of salts with a low solubility in the heavy liquid phase.
  • the average dimensions of the filling particles can be any suitable filling particles.
  • spheres with a diameter of 500 ⁇ m are preferred.
  • the distribution of the diameters can be well defined, distributed or bimodal . Larger particles can be charged, followed by finer particles .
  • the charging phase of the particles can be carried out in dry conditions or in the form of a slurry in the process liquid or other liquid.
  • the charging liquid if necessary, can be viscosized to help the suspension of the solid.
  • the charging and discharging phases of the filling can be automated. During the discharging, the filtered ob ⁇ structing solids possibly contained in the dispersion to be separated, are also expelled with the filling particles. The discharging of the complete contents of the rotor re- Jerusalem notes due to the fouling of the disks.
  • (1) represents the outer rotating skirt, (2) the inner skirt, (3) the perfo ⁇ rated separation element, (4) the closing base, (5) the gasket situated between the closing base and the outer skirt, (6) the feeding tube of the dispersion, non-rotating and coaxial with the tubular insert (7) which is part of the rotor.
  • the high part of the rotor (8) is integral with the outer skirt and equipped with a weir for the flow regu- lation of the two separated fluids which are expelled from the openings (9) and (10) .
  • the filling (11) in particle form is indicated by the shaded area.
  • the centrifuge is ac ⁇ tivated by rotating the conical skirts and closing the gas ⁇ ket by the feeding of water (17) .
  • the centrifuge is charged with the filtering particles (11) , and the fluid, or dis ⁇ persion, (12) is subsequently fed to the device through the tube (6) and tubular insert (7) .
  • the filling and fluid are forced against the walls of the inner skirt, thus obtaining the filtering action sice the oily component of the dispersion is re ⁇ tained by the filling particles.
  • the filtered water passes through the perforated separation element (3) , flows into the interspace (13) and, passing from the weir into (8) , is discharged through the opening (9) .
  • the oil, or oily phase, (14) accumulates in the central body (15) and, by centrifu ⁇ gal force, is discharged through the second opening (10) .
  • the arrows indicate the course of the fluid; the dark ar ⁇ rows represent the dispersion/concentrated oily phase, the light arrows the filtered water.
  • the feeding of the dispersion is stopped and the centrifuge is optionally slowed down.
  • the sealing gas ⁇ ket (5) is then released and the exhausted filtering bed can be discharged through the opening (16) , which is formed between the conical skirt and the closure bottom.
  • the sealing gasket situated on a specific support, not illustrated in the figure, is compressed against the periphery of the outer skirt by means of known methods.
  • the gasket and respective support are forced against the outer skirt by the thrust generated by the cen- trifugal force and maintained by the water circulation (17) .
  • the water feeding (17) is stopped and the release of the gasket causes the formation of the opening (16) .
  • the centrifuge can be charged again and reactivated. All the discharges expelled by centrifugation are collected in the channels positioned around the rotor and integral with the outer casing of the centrifuge (18) .
  • an experi- mental test is provided of the separation of a wa ⁇ ter/mineral oil dispersion by means of the centrifuge, ob ⁇ ject of the present invention, illustrated in the Figure.
  • the centrifuge modified for the tests is a medium-small sized centrifuge which can treat up to 500 1/h of liquid.
  • the equipment is suitable for continuous separations of the heavy phase (water) , light phase (oil) and solids and allows the regulation of the flow-rate ratios between the phases .
  • Oily water separation tests were carried out both in the laboratory, by using dispersions prepared artificially, and dispersions coming from an oil field.
  • the tests were effected using silicate spheres as filling particles, having an average diameter of 0.5 mm otherwise used for gravel pack in wells.
  • the tests were carried out by comparing the performances of the centri- fuge, object of the invention, and a conventional LAP X 202 disk centrifuge of ALFA LAVAL.
  • the fluid used was a disper ⁇ sion of oil in water with a concentration of 1,000 ppm.
  • the tests are compared after stabilization running for two hours at constant regime.
  • the conditions compared were the following: 4600 and 6600 rpm, 170 1/h of feeding, room temperature, without modifying the surface of the particles or with a hydrophizing silicone coating.
  • all the tests give the same results: the disk centrifuge separated the oil at 25-30 ppm whereas the cen ⁇ trifuge with the filling produced water containing only 8-12 ppm of oil.

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  • Physics & Mathematics (AREA)
  • Thermal Sciences (AREA)
  • Chemical & Material Sciences (AREA)
  • Chemical Kinetics & Catalysis (AREA)
  • Centrifugal Separators (AREA)
  • Solid-Sorbent Or Filter-Aiding Compositions (AREA)
  • Production Of Liquid Hydrocarbon Mixture For Refining Petroleum (AREA)
  • Treatment Of Liquids With Adsorbents In General (AREA)
  • External Artificial Organs (AREA)

Abstract

Porous bed centrifuge for the continuous separation of îm­miscible liquids, for example water and mineral oil/petroleum, obtained by a modification to conventional disk centrifuges for increasing their efficiency, wherein the disks have been substituted by a filling of solid par­ticles which act as a filtrating and coalescent bed.

Description

CONTINUOUS POROUS BED CENTRIFUGE
The present invention relates to a continuous porous bed centrifuge. More specifically, the present invention relates to a continuous porous bed centrifuge for the continuous separa¬ tion of immiscible liquids, for example water and mineral oil/petroleum, obtained by a modification to conventional disk centrifuges for increasing their efficiency. The disks have been substituted by a filling of solid particles which act as a filtrating and coalescent bed. Tests have been successfully carried out for deoiling of water associated with oil production.
Disk centrifuges are apparatuses used for the continu- ous or semi-continuous separation of liquids, possibly con¬ taining solid particles, baked on the action of centrifugal force on the fluid introduced into a rotor. For the modifi¬ cation object of the present invention, centrifuges are considered which allow the discharge of the heavy liquid phase (aqueous) . In order to automate the process and make it continuous, however, it is necessary to envisage the continuous discharge of the light phase (oil) and discharge of the solids. The inner part of rotors of conventional centrifuges generally contains truncated cone-shaped disks with spacers and holes for conveying the liquids. The heavy phase (liquid or solid) is concentrated in the outer part whereas the light phase tends to rise towards the rotation axis. The discharges of the two liquid phases leave the ro¬ tor and are collected by specific channels situated on the outer container. The discharge of the heavy liquid phase is controlled by a kind of weir (generally a disk with an in¬ ternal calibrated hole) depending on to the fluid and oper¬ ating conditions. The solids which accumulate in the rotor can be discharged at pre-established intervals. The com- plete discharge of the rotor is controlled by a washer ac¬ tivated by a hydraulic circuit which exploits the thrust generated by the centrifugal force.
In the upstream oil field, the large volumes involved and the cost are the main factors which limit the use of centrifuges, even if they have characteristics relating to efficiency, hindrance and flexibility in terms of feeding that can lead to their advantageous use in certain cases, for example on platforms.
The Applicants have now found that it is possible to provide various improvements to the purification process of layer water (heavy phase) which substantially reduces the concentrations of oil in waste water. It has been found, in fact, that it is possible to modify a conventional disk centrifuge by eliminating the disks and adapting the system so as to enable a filtrating filling to be charged and dis¬ charged during the rotation of the centrifuge. The modifi¬ cation introduced is aimed at forming a filtrating and coa- lescent bed subjected to centrifugal force in order to fa¬ vour the adhesion of the oil particles to the porous sur- face of the bed and separate them from the aqueous phase.
An object of the present invention therefore relates to a continuous porous bed centrifuge for the continuous separation of a fluid consisting of two immiscible liquids in dispersion, which comprises: a) a first outer compact essentially conical-shaped rotat¬ ing skirt; b) a second inner compact essentially conical-shaped skirt, integral with the outer skirt and positioned so as to form an interspace with said outer skirt; c) a perforated toroidal-shaped separation element posi¬ tioned at the base of the two skirts and suitable for separating the interspace from the inside of the centri¬ fuge; d) a closing base integral with the outer skirt by means of a sealing gasket;
_ T e) a section, equipped with a weir acting as a flow regula¬ tor, fixed at the head of the outer skirt and with open¬ ings for the discharge of the separated liquids; f) a first coaxial tube, integral with the outer skirt and with section (e) ; g) a second coaxial tube which is not integral with the outer skirt, positioned inside the first tube, for the feeding of the dispersion; h) a filling in the form of particles capable of filling from 40 to 70% of the inner volume of the centrifuge.
According to the present invention, the particle fill¬ ing is contained inside the rotating system and is kept separate from the interspace between the two skirts by means of the toroidal-shaped separation element which has a width which is substantially identical to the thickness of the interspace. The separation element can be a net, a small-holed grid or a septum with calibrated holes or pores in relation to the dimension of the particles of the fill¬ ing to be retained. The separation element is positioned in the area which is as far away as possible from the rotation axis so as to catch the heavier liquid (for example deoiled water) . Dur¬ ing the rotation of the centrifuge, the fed fluid is forced outwards by the centrifugal force and passes through the bed of particles and is filtered. The heavy phase con- sequently flows through the separation element (net) , passes into the cavity between the outer skirt and inner skirt and is discharged outside. Although subjected to cen¬ trifugal force, the filtering particles are withheld by the separation element.
The filtering and coalescent bed (filling) preferably consists of particles, for example sand, or spheres having different particle-sizes. The surfaces of the particles of the filling can be treated so as to have specific surface tension characteristics.
In particular, according to the present invention, the filling particles are spherical to favour their charging and discharging but can have any other shape, for example the form of cylinders, cubes, or other geometrical forms, balls of microfibers or generic sand.
The particles can be full or with cavities and the surfaces can be smooth or porous to increase the coales¬ cence effect .
The density of the solid particles must be greater than that of the light liquid phase. It is preferable but not compulsory for them to be even denser than the heavy liquid phase.
The particles are rigid and can be treated on the sur¬ face to change the wettability and favour the coalescence process and facilitate the detachment between the grains both in the discharging and charging phase. Silicone coat¬ ings and treatment with silanizing agents have been tested on silicate small spheres.
The particles can be made of glass, polymeric materi- als, metal, oxides (for example silica, silicates, alu¬ mina), ion exchange resins, zeolites, hollow glass micro¬ spheres, sands, diatomaceous earth, but also crystals of salts with a low solubility in the heavy liquid phase.
The average dimensions of the filling particles can
vary from 1 μm to 3 mm, determined by methods known to ex¬ perts in the field (for example, the Coulter method) . As
reference dimension, spheres with a diameter of 500 μm are preferred. The distribution of the diameters can be well defined, distributed or bimodal . Larger particles can be charged, followed by finer particles .
The charging phase of the particles can be carried out in dry conditions or in the form of a slurry in the process liquid or other liquid. The charging liquid, if necessary, can be viscosized to help the suspension of the solid. The charging and discharging phases of the filling can be automated. During the discharging, the filtered ob¬ structing solids possibly contained in the dispersion to be separated, are also expelled with the filling particles. The discharging of the complete contents of the rotor re- duces the necessity of frequent maintenance operations due to the fouling of the disks.
The continuous centrifuge, object of the present in¬ vention is now described with reference to the drawing of the enclosed figure which represents an illustrative and non-limiting embodiment, assuming a water/oil dispersion as process fluid.
With reference to the drawing, (1) represents the outer rotating skirt, (2) the inner skirt, (3) the perfo¬ rated separation element, (4) the closing base, (5) the gasket situated between the closing base and the outer skirt, (6) the feeding tube of the dispersion, non-rotating and coaxial with the tubular insert (7) which is part of the rotor. The high part of the rotor (8) is integral with the outer skirt and equipped with a weir for the flow regu- lation of the two separated fluids which are expelled from the openings (9) and (10) . The filling (11) in particle form is indicated by the shaded area. The functioning of the continuous centrifuge, object of the present invention, appears evident on the basis of the enclosed figure and the previous description. In particular, the centrifuge is ac¬ tivated by rotating the conical skirts and closing the gas¬ ket by the feeding of water (17) . The centrifuge is charged with the filtering particles (11) , and the fluid, or dis¬ persion, (12) is subsequently fed to the device through the tube (6) and tubular insert (7) . As a result of the cen- trifugal effect, the filling and fluid are forced against the walls of the inner skirt, thus obtaining the filtering action sice the oily component of the dispersion is re¬ tained by the filling particles. The filtered water passes through the perforated separation element (3) , flows into the interspace (13) and, passing from the weir into (8) , is discharged through the opening (9) . The oil, or oily phase, (14) accumulates in the central body (15) and, by centrifu¬ gal force, is discharged through the second opening (10) . The arrows indicate the course of the fluid; the dark ar¬ rows represent the dispersion/concentrated oily phase, the light arrows the filtered water.
When the filtering bed becomes blocked and must be substituted, the feeding of the dispersion is stopped and the centrifuge is optionally slowed down. The sealing gas¬ ket (5) is then released and the exhausted filtering bed can be discharged through the opening (16) , which is formed between the conical skirt and the closure bottom.
During the functioning of the centrifuge, the sealing gasket, situated on a specific support, not illustrated in the figure, is compressed against the periphery of the outer skirt by means of known methods. In the case illus¬ trated, the gasket and respective support are forced against the outer skirt by the thrust generated by the cen- trifugal force and maintained by the water circulation (17) . In the discharging phase, the water feeding (17) is stopped and the release of the gasket causes the formation of the opening (16) . After the closing of the gasket by re¬ establishing the water feeding (17) , the centrifuge can be charged again and reactivated. All the discharges expelled by centrifugation are collected in the channels positioned around the rotor and integral with the outer casing of the centrifuge (18) .
For illustrative and non-limiting reasons, an experi- mental test is provided of the separation of a wa¬ ter/mineral oil dispersion by means of the centrifuge, ob¬ ject of the present invention, illustrated in the Figure. The centrifuge modified for the tests is a medium-small sized centrifuge which can treat up to 500 1/h of liquid. The equipment is suitable for continuous separations of the heavy phase (water) , light phase (oil) and solids and allows the regulation of the flow-rate ratios between the phases .
Oily water separation tests were carried out both in the laboratory, by using dispersions prepared artificially, and dispersions coming from an oil field.
The tests were effected using silicate spheres as filling particles, having an average diameter of 0.5 mm otherwise used for gravel pack in wells. The tests were carried out by comparing the performances of the centri- fuge, object of the invention, and a conventional LAP X 202 disk centrifuge of ALFA LAVAL. The fluid used was a disper¬ sion of oil in water with a concentration of 1,000 ppm.
The tests are compared after stabilization running for two hours at constant regime. The conditions compared were the following: 4600 and 6600 rpm, 170 1/h of feeding, room temperature, without modifying the surface of the particles or with a hydrophizing silicone coating. In spite of the variables, all the tests give the same results: the disk centrifuge separated the oil at 25-30 ppm whereas the cen¬ trifuge with the filling produced water containing only 8-12 ppm of oil.
Eight hour long tests were carried out in the field at 6600 rpm and 170 1/h of feeding, the water came from a three-phase separator, the temperature was 45°C, measured at the outlet of the centrifuge, the oil content in the dispersion oscillated between 300 and 700 ppm. All the sam¬ plings of the outgoing water, effected at different times, gave 18-20 ppm of oil with the disk centrifuge and 6-7 ppm with the modified centrifuge.

Claims

1. A continuous porous bed centrifuge for the continuous separation of a fluid consisting of two immiscible liquids in dispersion, which comprises: a) a first outer compact essentially conical-shaped rotat¬ ing skirt; b) a second inner compact essentially conical-shaped skirt, integral with the outer skirt and positioned so as to form an interspace with said outer skirt; c) a perforated toroidal-shaped separation element posi¬ tioned at the base of the two skirts and suitable for separating the interspace from the inside of the centri¬ fuge; d) a closing base integral with the outer skirt by means of a sealing gasket; e) a section, equipped with a weir acting as a flow regula¬ tor, fixed at the head of the outer skirt and with open¬ ings for the discharge of the separated liquids; f) a first coaxial tube, integral with the outer skirt and with section (e) ; g) a second coaxial tube which is not integral with the outer skirt, positioned inside the first tube, for the feeding of the dispersion; h) a filling in the form of particles capable of filling from 40 to 70% of the inner volume of the centrifuge.
2. The centrifuge according to claim 1, wherein the fill¬ ing preferably consists of particles or spheres having dif¬ ferent particle-sizes, optionally treated so as to have specific surface tension characteristics.
3. The centrifuge according to claim 1 or 2, wherein the filling particles are spherical.
4. The centrifuge according to claim 1 or 2, wherein the filling particles are in the form of cylinders, cubes, balls of microfibers .
5. The centrifuge according to claim 1 or 2, wherein the filling particles consist of sand.
6. The centrifuge according to claim 1 or 2, wherein the filling particles are full or with a cavity and the sur¬ faces are either smooth or porous.
7. The centrifuge according to claim 1 or 2, wherein the filling particles have a density greater than that of the light liquid phase.
8. The centrifuge according to claim 1 or 2, wherein the filling particles are glass, polymeric materials, metal, oxides, ion exchange resins, zeolites, hollow glass micro¬ spheres, sands, infusorial earth, crystals of salts with a low solubility in the heavy liquid phase.
9. The centrifuge according to claim 1 or 2, wherein the
filling particles have average dimensions ranging from 1 μm to 3 mm.
PCT/EP2005/011807 2004-11-08 2005-11-03 Continuous porous bed centrifuge WO2006048299A1 (en)

Priority Applications (12)

Application Number Priority Date Filing Date Title
EP05800671A EP1809423B1 (en) 2004-11-08 2005-11-03 Continuous porous bed centrifuge
MX2007005539A MX2007005539A (en) 2004-11-08 2005-11-03 Continuous porous bed centrifuge.
AU2005300696A AU2005300696B2 (en) 2004-11-08 2005-11-03 Continuous porous bed centrifuge
BRPI0517447-3A BRPI0517447A (en) 2004-11-08 2005-11-03 continuous porous bed centrifuge for continuous separation of a fluid consisting of two immiscible liquids in dispersion
EA200700612A EA010536B1 (en) 2004-11-08 2005-11-03 Continuous porous bed centrifuge
AT05800671T ATE518597T1 (en) 2004-11-08 2005-11-03 CONTINUOUS POROUS BED CENTRIFUGE
US11/577,992 US7708681B2 (en) 2004-11-08 2005-11-03 Continuous porous bed centrifuge
CA2581416A CA2581416C (en) 2004-11-08 2005-11-03 Continuous porous bed centrifuge
DK05800671.9T DK1809423T3 (en) 2004-11-08 2005-11-03 Centrifuge with continuous, porous bearing
PL05800671T PL1809423T3 (en) 2004-11-08 2005-11-03 Continuous porous bed centrifuge
NO20072143A NO20072143L (en) 2004-11-08 2007-04-25 Centrifuge with continuous, porous mass
EGNA2007000416 EG24700A (en) 2004-11-08 2007-04-26 Continuous porous bed centrifuge

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IT002137A ITMI20042137A1 (en) 2004-11-08 2004-11-08 CENTRIFUGE CONTINUES WITH POROUS BED
ITMI2004A002137 2004-11-08

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AU (1) AU2005300696B2 (en)
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EA (1) EA010536B1 (en)
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ES (1) ES2370831T3 (en)
IT (1) ITMI20042137A1 (en)
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WO2009095241A1 (en) * 2008-01-28 2009-08-06 Eni S.P.A. Continuous porous bed centrifuge
WO2010012656A1 (en) * 2008-07-31 2010-02-04 Shell Internationale Research Maatschappij B.V. Process for separating liquid mixtures
CN105300108A (en) * 2015-10-22 2016-02-03 桐乡市耀润电子有限公司 Blanking equipment used for feeding ferrite spherical particle raw materials into pre-sintering kiln
CN105333737A (en) * 2015-10-22 2016-02-17 桐乡市耀润电子有限公司 Discharging device used before ferrite spherical particle raw materials enter presintering kiln
TWI688429B (en) * 2019-01-15 2020-03-21 賴沛琪 Deoiling treatment device
CN117865282A (en) * 2024-03-13 2024-04-12 成都天府智慧大厨房科技有限责任公司 Kitchen garbage oil-water separation device

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WO2010096645A2 (en) * 2009-02-20 2010-08-26 H R D Corporation Apparatus and method for gas separation
AU2012211392B2 (en) 2011-08-29 2014-11-20 Process Group Pty Ltd Compact Separation Apparatus
US10301196B2 (en) 2013-06-15 2019-05-28 Exactration, Llc Skimmer and oil water separator
US10611649B2 (en) 2016-12-06 2020-04-07 Exactration, Llc Skimmer and oil water separator process
CN105300107B (en) * 2015-10-22 2017-07-21 桐乡市耀润电子有限公司 Enter the doffer of pre- firing for ferrite ball type particulate material
CN112957772B (en) * 2021-02-04 2022-10-18 无锡力必特自动化设备有限公司 Fluid filter and filtering method
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WO2010012656A1 (en) * 2008-07-31 2010-02-04 Shell Internationale Research Maatschappij B.V. Process for separating liquid mixtures
CN105300108A (en) * 2015-10-22 2016-02-03 桐乡市耀润电子有限公司 Blanking equipment used for feeding ferrite spherical particle raw materials into pre-sintering kiln
CN105333737A (en) * 2015-10-22 2016-02-17 桐乡市耀润电子有限公司 Discharging device used before ferrite spherical particle raw materials enter presintering kiln
CN105300108B (en) * 2015-10-22 2017-07-21 桐乡市耀润电子有限公司 Enter the blanking device of pre- firing for ferrite ball type particulate material
TWI688429B (en) * 2019-01-15 2020-03-21 賴沛琪 Deoiling treatment device
CN117865282A (en) * 2024-03-13 2024-04-12 成都天府智慧大厨房科技有限责任公司 Kitchen garbage oil-water separation device
CN117865282B (en) * 2024-03-13 2024-05-14 成都天府智慧大厨房科技有限责任公司 Kitchen garbage oil-water separation device

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ATE518597T1 (en) 2011-08-15
CA2581416C (en) 2013-01-08
EA010536B1 (en) 2008-10-30
PL1809423T3 (en) 2011-12-30
CA2581416A1 (en) 2006-05-11
DK1809423T3 (en) 2011-11-21
EG24700A (en) 2010-05-26
EP1809423A1 (en) 2007-07-25
ES2370831T3 (en) 2011-12-23
US20090139921A1 (en) 2009-06-04
EP1809423B1 (en) 2011-08-03
AU2005300696A1 (en) 2006-05-11
MX2007005539A (en) 2007-07-25
NO20072143L (en) 2007-08-01
US7708681B2 (en) 2010-05-04
ITMI20042137A1 (en) 2005-02-08
AU2005300696B2 (en) 2010-05-06
BRPI0517447A (en) 2008-10-07
PT1809423E (en) 2011-11-15
EA200700612A1 (en) 2007-10-26

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