NL2004559C2 - Device and method for coalescing droplets dispersed in a flowing mixture. - Google Patents
Device and method for coalescing droplets dispersed in a flowing mixture. Download PDFInfo
- Publication number
- NL2004559C2 NL2004559C2 NL2004559A NL2004559A NL2004559C2 NL 2004559 C2 NL2004559 C2 NL 2004559C2 NL 2004559 A NL2004559 A NL 2004559A NL 2004559 A NL2004559 A NL 2004559A NL 2004559 C2 NL2004559 C2 NL 2004559C2
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- NL
- Netherlands
- Prior art keywords
- flow channels
- mixture
- assembly
- flow
- rotating
- Prior art date
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- 239000000203 mixture Substances 0.000 title claims description 71
- 238000000034 method Methods 0.000 title claims description 32
- XLYOFNOQVPJJNP-UHFFFAOYSA-N water Substances O XLYOFNOQVPJJNP-UHFFFAOYSA-N 0.000 claims description 34
- 239000007788 liquid Substances 0.000 claims description 24
- 238000000926 separation method Methods 0.000 claims description 14
- 238000004581 coalescence Methods 0.000 claims description 6
- 238000007599 discharging Methods 0.000 claims description 4
- 230000002093 peripheral effect Effects 0.000 claims 3
- 239000006185 dispersion Substances 0.000 description 4
- 230000005484 gravity Effects 0.000 description 3
- 239000000463 material Substances 0.000 description 3
- 230000001105 regulatory effect Effects 0.000 description 3
- 239000012223 aqueous fraction Substances 0.000 description 2
- 230000000694 effects Effects 0.000 description 2
- 238000009434 installation Methods 0.000 description 2
- 239000003129 oil well Substances 0.000 description 2
- 239000002245 particle Substances 0.000 description 2
- 239000007787 solid Substances 0.000 description 2
- 239000002699 waste material Substances 0.000 description 2
- TVEXGJYMHHTVKP-UHFFFAOYSA-N 6-oxabicyclo[3.2.1]oct-3-en-7-one Chemical compound C1C2C(=O)OC1C=CC2 TVEXGJYMHHTVKP-UHFFFAOYSA-N 0.000 description 1
- 230000032683 aging Effects 0.000 description 1
- 230000009286 beneficial effect Effects 0.000 description 1
- 230000015572 biosynthetic process Effects 0.000 description 1
- 230000001186 cumulative effect Effects 0.000 description 1
- 238000009826 distribution Methods 0.000 description 1
- 239000000839 emulsion Substances 0.000 description 1
- 239000003822 epoxy resin Substances 0.000 description 1
- 238000002474 experimental method Methods 0.000 description 1
- 238000000605 extraction Methods 0.000 description 1
- 230000002349 favourable effect Effects 0.000 description 1
- 239000012530 fluid Substances 0.000 description 1
- ZZUFCTLCJUWOSV-UHFFFAOYSA-N furosemide Chemical compound C1=C(Cl)C(S(=O)(=O)N)=CC(C(O)=O)=C1NCC1=CC=CO1 ZZUFCTLCJUWOSV-UHFFFAOYSA-N 0.000 description 1
- 239000012535 impurity Substances 0.000 description 1
- 238000002347 injection Methods 0.000 description 1
- 239000007924 injection Substances 0.000 description 1
- 239000000543 intermediate Substances 0.000 description 1
- 230000003189 isokinetic effect Effects 0.000 description 1
- 210000003041 ligament Anatomy 0.000 description 1
- 238000004519 manufacturing process Methods 0.000 description 1
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- 230000000704 physical effect Effects 0.000 description 1
- 229920000647 polyepoxide Polymers 0.000 description 1
- 230000002028 premature Effects 0.000 description 1
- 239000008213 purified water Substances 0.000 description 1
- 238000011084 recovery Methods 0.000 description 1
- 238000010008 shearing Methods 0.000 description 1
- 239000011343 solid material Substances 0.000 description 1
- 229910001220 stainless steel Inorganic materials 0.000 description 1
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Classifications
-
- 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
Landscapes
- Physics & Mathematics (AREA)
- Thermal Sciences (AREA)
- Chemical & Material Sciences (AREA)
- Chemical Kinetics & Catalysis (AREA)
- Centrifugal Separators (AREA)
Description
Device and method for coalescing droplets dispersed in a flowing mixture
The invention relates to a device for coalescing droplets dispersed in a flowing mixture of at least two liquids with different mass density. The invention also relates to a 5 method for coalescing droplets dispersed in a flowing mixture of at least two liquids with different mass density, and to a method for separating a mixture of at least two liquids with different mass density into at least two fractions that each substantially comprise one of the at least two liquids.
10 Oil producers are increasingly facing problems with large amounts of water present in oil wells, in particular ageing oil wells. As a well matures, the amount of water in the oil may reach 90% and more. The two liquids (water and oil) being substantially immiscible or non-soluble in one another form a dispersion of rather small oil droplets in a continuous water phase (or vice versa). The main concern for the oil producer is to 15 be able to efficiently separate the oil droplets from the water phase with a high selectivity, thereby obtaining high quality oil with a low amount of water. On the other hand, he needs to dispose of the water, and this disposal has to meet increasingly stringent standards of quality. There is therefore a need for a method that is able to separate a mixture of at least two liquids with different mass density (such as oil and 20 water) into at least two fractions that each substantially comprise one of the at least two liquids.
Gravity separators are commonly used to separate dispersions and emulsions into their components. In such equipment, differences in densities of the two liquids cause 25 droplets to rise or fall by their buoyancy. The greater the difference in densities, the easier the separation becomes. In order to settle fine droplets and ensure laminar flow, large vessels and long residence times are required. It may take five, ten, and or even thirty minutes to make a separation, depending on the physical properties of the mixture stream. If this time is not available, hazy, off spec products or intermediates that cause 30 problems in downstream equipment are obtained.
Liquid-liquid coalescers are used to accelerate the merging of many droplets to form a lesser number of droplets, but with a greater diameter. This increases the buoyant forces and settling of the larger droplets downstream of the coalescer element then requires 2 less residence time. A known type of coalescers depends on settling of droplets and confine the distance a droplet can rise or fall between parallel plates or crimps of packing sheets. Another type depends on interception of droplets and uses a multiplicity of fine wires or filaments to collect fine droplets as they travel in the laminar flow 5 streamlines around them. An essential step in coalescers is to combine, aggregate, or coalesce captured droplets. This actual coalescing step is a complex function of surface tension and viscous effects, droplet momentum, and the dynamics of the sizes of the droplets in the dispersion.
10 Although the known coalescers accelerate the subsequent separation process in a gravity separator, there remains room for improvement, both with respect to the speed of separation and with respect to its selectivity. This is in particular the case when coalescing oil droplets dispersed in a mixture of oil and water.
15 The invention provides for this purpose a device for coalescing droplets dispersed in a flowing mixture of at least two liquids with different mass density, the device comprising: rotating means in the form of a rotating assembly of flow channels that are accessible to the flowing mixture, 20 - pressure means for forcing the mixture through the flow channels, an inlet for the mixture connecting to the rotating means, and an outlet connecting to the rotating means for discharging the coalesced mixture, wherein the smallest distance between the inner walls of two flow channels is larger than 30 micron.
25
As a result of the rotation of the assembly of flow channels, the lighter fraction of the mixture (which corresponds to the oil fraction in a water/oil mixture) will migrate at least substantially to the inner side of the flow channels (the side closest to the center of rotation) and coalesce at this side, for instance in the form of a film, while the heavier 30 fraction (which corresponds to the water fraction in a water/oil mixture) will migrate at least substantially to the outer side of the flow channels. The coalesced lighter fraction breaks up into droplets at the downstream end of the flow channels. Due to the fact that the assembly of flow channels is designed such that the smallest distance between the inner walls of two flow channels is larger than 30 micron, the lighter fraction is 3 collected at the end of the flow channels as droplets that are substantially larger than the incoming average droplet size prior to rotating.
In a preferred embodiment, the device is characterized in that the assembly of flow 5 channels is designed such that the smallest distance between the inner walls of two flow channels is larger than 50 micron, even more preferred larger than 70 micron, and most preferred larger than 100 micron.
The device is typically able to coalesce micron-sized droplets dispersed in a flowing 10 mixture to droplets that may be 10 to 50 times as large as the incoming average droplet size, without having to use voluminous equipment (i.e. the device can take a very compact form). Moreover, the mixture has to be treated in the device for a short period of time only to achieve the effect.
15 The rotating coalescer in the form of a rotating assembly of flow channels has the advantage that the average distance in the radial direction of the mixture from a wall is limited. Since the flow channels are many and of small size, a coalesced layer may readily be achieved in a relatively short time and with a high throughput, even when the available length of the flow channels is relatively limited (corresponding to the length in 20 the axial direction of the rotating assembly). The flow speeds of the mixture to be applied in the flow channels may be varied or optimised according to the properties of the mixture.
Although the number of flow channels can in principle be chosen within wide limits, it 25 is recommended that the number of flow channels in the assembly is at least 500, more preferably at least 800 and most preferably at least 1000. The flow channels of the rotating means of the device may have any desired form. It is thus possible to have them run in a random curve in the lengthwise direction or, conversely, make them almost linear. The flow channels in the assembly preferably extend substantially linear and 30 mutually parallel to the axis of rotation of the assembly.
The space between the flow channels in the assembly of flow channels may be accessible or inaccessible to the flowing mixture, for instance by being filled with material, thereby leaving the flow channels accessible to the flowing mixture only. In an 4 embodiment wherein the space between the flow channels in the assembly of flow channels is accessible to the flowing mixture, this space is not or only partly filled up with material. The assembly may for instance comprise a number of cylindrical flow channels that have been stacked in parallel to each other according to some stacking 5 order, and the interstitial space filled up with a hardening material, such as an epoxy resin for instance. It is clear that the invention is not limited to this particular production method and other methods are equally well applicable. In such case, a cross-section of the assembly comprises a number of circular flow channel cross-sections arranged according to some array, such as a rectangular or hexagonal array for instance, with the 10 interstitial space optionally filled with solid material. The smallest distance between the inner walls of two flow channels in such case corresponds to twice the wall thickness of the follow channels.
In another preferred embodiment of the invention, a device is provided wherein the total 15 inaccessible cross-sectional area of the rotating assembly of flow channels exceeds 20% of the total accessible cross-sectional area thereof. The total inaccessible cross-sectional area of the assembly is the sum of all filled-up interstitial areas, whereas the total accessible cross-sectional area of the assembly is the total flow-through area, i.e. the sum of the cross-sectional areas of the flow channels. The present embodiment produces 20 a coalesced mixture having an increased ratio of average droplet size at the outlet to the average droplet size at the inlet.
Even more preferred is a device, wherein the total inaccessible cross-sectional area of the rotating assembly of flow channels exceeds 30%, more preferred 35% and most 25 preferred 40% of the total accessible cross-sectional area thereof.
A preferred variant of the device according to the invention comprises flow channels with singly-connected cross-section. In a first variant this is understood to mean that each flow channel has a cross-section extending along practically the whole length 30 thereof which extends azimuthally around the axis of rotation at an angle smaller than 360° such that the azimuthal flow at an angle greater than 360° to the axis of rotation is substantially prevented. In a second variant a singly-connected cross-section is understood to mean that each flow channel extends azimuthally around the axis of rotation at an angle smaller than 360° such that azimuthal flow at an angle greater than 5 360° to the axis of rotation is substantially prevented in each flow channel, wherein each flow channel is provided with wall portions extending substantially along the total length thereof, wherein the coalescence is bounded in radial and azimuthal directions relative to the axis of rotation. In a third variant a singly-connected cross-section is 5 understood to mean that each flow channel extends azimuthally around the axis of rotation at an angle smaller than 360° such that azimuthal flow at an angle greater than 360° to the axis of rotation is substantially prevented in each flow channel, wherein each flow channel is enclosed by a single wall extending substantially along the whole length thereof.
10
The invention also relates to a method for coalescing droplets dispersed in a flowing mixture of at least two liquids with different mass density. The method comprises the steps of: A) providing rotating means in the form of a rotating assembly of flow channels 15 according to the invention, B) supplying a mixture of at least two liquids with different mass density through an inlet that connects to the rotating means, C) forcing the mixture through the flow channels of the rotating means, thereby causing the flowing mixture to rotate, and 20 D) discharging the mixture through an outlet connecting to the rotating means.
In another embodiment of the invention, a method is provided wherein the rotational speed of the rotating assembly of flow channels and the pressure for forcing the mixture through the flow channels are regulated such that the ratio of the circumferential 25 velocity in a flow channel furthest away from the center of rotation of the assembly to the average axial velocity in the flow channels ranges from 30 to 450, more preferred from 40 to 200, and most preferred from 50 to 100. The preferred ranges allow to coalesce incoming droplets as small as 1 micron, even for a mixture wherein the two liquids differ in mass density to a small extent only. A typical example of a liquid/liquid 30 mixture wherein the two liquids differ in mass density to a small extent only is an oil/water mixture.
In particular with such mixtures, any flow disturbance in the flow channels may disrupt or negatively affect the coalescence of the lighter fraction on the inner walls of the 6 channels. At higher rotational speeds for instance, any component of the rotation in the plane perpendicular to the axis of the flow channels can cause a Coriolis force, whereby an internal eddying is created in the flow channels in the plane perpendicular to the channel axis. The method and device according to the invention are adapted to diminish 5 or even prevent such disturbances.
It has also been found that coalescence is improved in an embodiment of the method wherein the rotational speed of the flow channels are regulated such that the ratio of the centrifugal pressure in a flow channel furthest away from the center of rotation of the 10 assembly to the average axial pressure drop over the flow channels ranges from 20 to 200, whereby the centrifugal pressure is given by pQ2Ro2/2 and the average axial pressure drop by 32(iLu/dc 15 wherein Q denotes the rotational speed of the assembly, \x represents the dynamic viscosity of the mixture, u denotes the average axial velocity in the flow channels, and Ro, L and dc represent the largest distance to the center of rotation of the assembly (for a cylindrical assembly of flow channels this corresponds to the radius of the assembly), the length of the flow channels, and the hydraulic diameter of the flow channels 20 respectively.
Even more preferred is an embodiment of the method wherein the rotational speed of the flow channels is regulated such that the ratio of the centrifugal pressure in a flow channel furthest away from the center of rotation of the assembly to the average axial 25 pressure drop over the flow channels ranges from 30 to 100.
Another embodiment of the method according to the invention is characterized in that the flow in the flow channels is substantially laminar. In order to ensure laminar flow in the flow channels, the process conditions and the channel dimensions are chosen such 30 that the Reynolds number is significantly lower than 2000, and generally amounts to about 1000.
The invention further relates to a method for separating a mixture of at least two liquids with different mass density into at least two fractions that each substantially comprise 7 one of the at least two liquids, the method comprising coalescing droplets dispersed in the flowing mixture according to the method described above, and thereafter subjecting the mixture thus obtained to a conventional separation. The subsequent separation is not limited to any separation method in particular and may be a gravity separator, a 5 centrifugal separator, a (hydro)cyclone, a plate pack separator, and the like. By coalescing the mixture according to the invented method and using the invented device prior to actual separation, the efficiency and selectivity of said separation may be enhanced considerably.
10 The present invention will be further elucidated on the basis of the non-limitative exemplary embodiments shown in the following figures. Herein: figure 1 shows a schematic view in perspective of a device according to the invention, figure 2 schematically shows an enlarged part of a cross section of the rotating assembly of flow channels according to line A-A of the device of figure 1, 15 figure 3 represents a graph of the efficiency of the coalescing process carried out in a device according to the invention, and figure 4 represents a table of experimental results obtained for a number of Examples of the method according to the invention.
20 With reference to figure 1 a device 1 for coalescing oil droplets dispersed in a flowing water/oil mixture is shown. Device 1 comprises a cylindrical housing 2 confined by an upstream end plate 3 and a downstream end plate 4. The housing comprises rotating means in the form of a rotating assembly 5 of flow channels 6, arranged mutually parallel to an axis of rotation 7. The rotation axis 7 is supported by bearings 8 and 9 that 25 are provided in end plates 3 and 4 respectively. Device 1 is further provided with an inlet 10 that tangentially connects to the rotating means through an entrance chamber 11. In the entrance chamber 11 the oil/water mixture is accelerated to the desired angular velocity, and the swirling mixture also drives the rotating assembly 5. Another possibility is to drive the rotating assembly 5 by a motor. The oil/water mixture is 30 pumped through the inlet 10 by pressure means in the form of an hydraulic pump (not shown) for forcing the mixture through the flow channels 6. The entrance chamber 11 is further provided with a static blade 12 which helps in adjusting the flow of water to allow a smooth entry into the rotating assembly 5. Entrance chamber 11 is also 8 instrumental in separating out any solid particles that may be present in the water to prevent clogging of the flow channels 6.
The cross-section of rotating assembly 5 according to the line A-A is shown in enlarged 5 view in figure 2. The flow channels 6 occupy a part of the cross-section which is accessible to the flowing oil/water mixture, while the part between the flow channels 6 is inaccessible to the flowing mixture. This inaccessible part 20 is hatched in figure 2 and may be manufactured from stainless steel for instance. According to an embodiment of the invention, the total inaccessible cross-sectional area 20 of the rotating assembly 5 10 of flow channels 6 exceeds 20% of the total accessible cross-sectional area thereof (the sum of the areas of all flow channels 6), and more preferred exceeds 40% of the total accessible cross-sectional area of the rotating assembly 5. In case the flow channels are regularly distributed over the cross-section of rotating assembly 5 (which is preferred) this ensures a minimum thickness of the ligaments between the flow channels 6. It was 15 found that this measure is beneficial to the formation of relatively large droplets at the downstream side of the rotating assembly 5 and therefore to coalescence efficiency. A particularly favourable rotating assembly 5 comprises flow channels 6 for which the smallest distance 21 between the inner walls of two flow channels 6 is larger than 30 micron, and more preferred larger than 50 micron.
20
In the assembly 5 of flow channels 6, oil droplets are centrifuged to the inner wall (the wall part closest to the center of rotation) of each channel 6. Oil droplets hit the wall of a channel and coalesce into a film 22 that moves thickens in the downstream direction of the assembly 5. Oil depleted water 23 flows through the remaining cross-section of 25 the channels 6. Upon reaching the end of the channels 6, the coalesced film 22 breaks-up into droplets under the influence of the centrifugal forces. The droplets thus produced have a larger average size than the average droplet size at the inlet 10.
Device 1 may operate at widely varying flow rates but typically operates at a volume 30 flow of 20 m3/hr for instance, while rotating at a rotational speed of 1500 rpm. The pressure means are typically able to produce pressures of up to 30 bar, although higher pressures may be envisaged.
9
Device 1 further comprises an outlet 14 connecting downstream to the rotating assembly 5 via separation chamber 13. Chamber 13 acts as an axial centrifuge and is entirely filled with fluid, in casu the oil/water mixture. The large oil droplets as produced by the assembly 5 of flow channels 6 are collected around the axis 7 of the 5 assembly 5 while the oil-depleted (cleaned) water is forced to leave the assembly 5 at the outer radius at outlet 14. This water is then available for further separation in conventional installations such as plate pack separators, IGF installations and/or hydrocyclones. Separation chamber 13 may comprise blades (not shown) and other means that minimize secondary flows and turbulence, since these may disrupt the 10 formed coalesced droplets and disturb the separation of the oil from the water fraction. At the outlet, the heavy fraction comprises purified water with a minor component of residual oil, while the lighter fraction comprises a dispersion of oil and water, in which the oil is present as relatively large droplets, allowing for easy recovery of this ‘waste’ oil fraction. This oil fraction is led through an outlet 15 to a suitable separator, which 15 may be a centrifugal separator 16 or any other conventional separator for recovering the waste oil, or directly to a container.
A specific embodiment of a device 1 according to the invention has been used for a number of experiments that demonstrate the invented method. This specific 20 embodiment uses flow channels with a diameter dc = 1,5 mm, and a length L = 200 mm. The outer radius of the rotating assembly 5 is Ro = 300 mm, while its inner radius is Ri = 150 mm. Device 1 was further equipped with two 30 m3 buffer tanks allowing for continuous operating of the device and a precise oil-injection system combined with a disrupting mechanism to create the desired oil cut and oil droplet size. To the oil-25 depleted water outlet 14 was connected a Facet Industries highly efficient M-Pak® coalescing plate separator.
It was observed that with a flow rate of 20 m3/hr and a rotational velocity of assembly 5 of 1500 rpm, oil droplets with a dpso of 4,6 micron are readily coalesced in the assembly 30 5. The dpso is defined as the droplet size that has a 50% probability to be coalesced in the assembly of the given length and channel diameter. A cumulative probability plot 30 of the coalesced droplets is shown in figure 3 against the droplet size 32, showing that droplets of 7,9 micron and larger have a probability of 90% to coalesce in the assembly 5 to form coalesced oil droplets with a size distribution 31 (dP9o = 7,9 micron).
10
Tests were performed with a clean water volume flow between 10 and 20 m3/hr, oil inlet concentrations adjustable from 50 to 300 ppm, and rotational velocities of the assembly 5 ranging from 750 to 1000 rpm. Iso-kinetic sample points were available to 5 take samples from the flow to determine the oil content. The samples were taken at the inlet 10, at a location in the entrance chamber 11 just prior to entry into the assembly 5 of flow channels 6, and at the heavy fraction (oil depleted clean water) outlet 14. The samples were analysed for oil content (hexane-extraction). .
10 For velocities of 750, 1000 and 1500 rpm, the break-up droplet diameter was observed to be 465, 349 and 232 micron respectively. For the standard operating conditions (1500 rpm, 20 m3/hr) as shown in figure 3, the droplets are therefore enlarged 25 times (from 9,3 to 232 micron). The velocity could be raised up to 7000 rpm to obtain a break-up droplet size of 50 micron still. However, due to the high rotational velocity, further 15 break-up of the droplets downstream of the assembly 5 does occur.
The test results are shown in the table of figure 4. In the first series of tests (test 1 to 5), the device was utilized as a single, standalone coalescing unit, with a focus on achieving a low oil concentration in the water outlet 14. These tests show that at the inlet 10 the 20 average oil concentration is about 70 ppm and that this concentration is effectively reduced to an average concentration of about 4 ppm at the outlet 14.
In the second series of tests (tests 6 and 7), the influence of different settings such as droplet size and flow split was tested. It confirmed that with smaller droplets at the inlet 25 10, the oil concentration at the outlet 14 rises. Further, higher inlet concentrations resulted in lower performance.
The third series of tests (tests 8 and 9) was performed with the Facet plate separator connected to the water outlet 14 of device 1. Only part of the water outlet flow was 30 connected to the plate separator, as it was designed to have a volume flow of 1 m3/hr maximum. The tests were performed with a volume flow rate of 750 1/hr through the plate separator. It showed good results, as oil concentrations after the plate separator are very low.
11
Visual inspection of the flow channels 6 of assembly 5 showed no sign of clogging.
From the results, it can be concluded that the device according to the invention effectively reduces the oil content in an oil/water mixture by more than 90 %, while at 5 the same time creating an oil/water mixture with relatively large oil droplets available for downstream separators. Droplets larger than 4,6 micron are separated with a 50% probability and coalesced into droplets of 230 micron and larger. Droplets are enlarged up to 25 times in the device of the invention. Thousands of channels each function as a small centrifuge, resulting in high throughputs while maintaining a high efficiency.
10
By providing the inlet and outlet sections of the device with arrangements such as blades allow to minimize shearing and premature break-up of oil droplets. The device has a large operating window and may maintain a constant high efficiency level. It also has the possibility to separate impurities such solids and heavy particles from the 15 oil/water mixture prior to entering the flow channels of the rotating assembly.
Claims (13)
Priority Applications (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL2004559A NL2004559C2 (en) | 2010-04-15 | 2010-04-15 | Device and method for coalescing droplets dispersed in a flowing mixture. |
| PCT/NL2011/050256 WO2011129697A1 (en) | 2010-04-15 | 2011-04-14 | Device and method for coalescing droplets dispersed in a flowing mixture |
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| NL2004559A NL2004559C2 (en) | 2010-04-15 | 2010-04-15 | Device and method for coalescing droplets dispersed in a flowing mixture. |
| NL2004559 | 2010-04-15 |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| NL2004559C2 true NL2004559C2 (en) | 2011-10-18 |
Family
ID=42357823
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| NL2004559A NL2004559C2 (en) | 2010-04-15 | 2010-04-15 | Device and method for coalescing droplets dispersed in a flowing mixture. |
Country Status (2)
| Country | Link |
|---|---|
| NL (1) | NL2004559C2 (en) |
| WO (1) | WO2011129697A1 (en) |
Families Citing this family (5)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US11118218B2 (en) | 2012-09-12 | 2021-09-14 | Cypho, Inc. | Common port emulsion generation system |
| US20140193857A1 (en) * | 2012-09-12 | 2014-07-10 | Cypho, Inc. | Centrifuge tube droplet generator |
| EP2735351B1 (en) | 2012-11-23 | 2014-12-31 | Alfa Laval Corporate AB | Centrifugal separator for separating particles from a gas stream |
| EP2735352A1 (en) | 2012-11-23 | 2014-05-28 | Alfa Laval Corporate AB | A centrifugal separator |
| US12023637B2 (en) | 2020-03-23 | 2024-07-02 | Mark A. Gray | Capillary tube droplet generation systems and methods |
Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US507442A (en) * | 1893-10-24 | Atto lentsch | ||
| US3695509A (en) * | 1969-08-08 | 1972-10-03 | Termomeccanica Italiana Spa | Centrifugal separator for separating emulsions |
| US3931927A (en) * | 1973-01-12 | 1976-01-13 | Standard Oil Company | Centrifuge |
| US6083147A (en) * | 1995-07-25 | 2000-07-04 | Centritech Hb | Apparatus and method for discontinuous separation of solid particles from a liquid |
| US20060225386A1 (en) * | 2005-02-17 | 2006-10-12 | Bert Brouwers | Method for removing contaminating gaseous components from a natural gas stream |
| US20090301296A1 (en) * | 2006-02-23 | 2009-12-10 | Romico Hold A.V.V. | Device and method for separating a flowing medium mixture into fractions |
-
2010
- 2010-04-15 NL NL2004559A patent/NL2004559C2/en not_active IP Right Cessation
-
2011
- 2011-04-14 WO PCT/NL2011/050256 patent/WO2011129697A1/en not_active Ceased
Patent Citations (6)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| US507442A (en) * | 1893-10-24 | Atto lentsch | ||
| US3695509A (en) * | 1969-08-08 | 1972-10-03 | Termomeccanica Italiana Spa | Centrifugal separator for separating emulsions |
| US3931927A (en) * | 1973-01-12 | 1976-01-13 | Standard Oil Company | Centrifuge |
| US6083147A (en) * | 1995-07-25 | 2000-07-04 | Centritech Hb | Apparatus and method for discontinuous separation of solid particles from a liquid |
| US20060225386A1 (en) * | 2005-02-17 | 2006-10-12 | Bert Brouwers | Method for removing contaminating gaseous components from a natural gas stream |
| US20090301296A1 (en) * | 2006-02-23 | 2009-12-10 | Romico Hold A.V.V. | Device and method for separating a flowing medium mixture into fractions |
Also Published As
| Publication number | Publication date |
|---|---|
| WO2011129697A1 (en) | 2011-10-20 |
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