CN203886239U - System for removing water from oil - Google Patents

Abstract

The utility model relates to a system for separating discontinuous and continuous phases of emulsion. According to the system, the mass density of the liquid in the discontinuous phase is higher than that of the liquid in the continuous phase. The system comprises a plurality of channels (100), wherein each channel (100) horizontally stretches from a feeding opening (101) to a discharging opening (103); each feeding opening (101) is communicated with inlets (301 and 401) via an inlet manifold (202) to distribute fluid flow received from the inlets (301 and 401) into the channels (100), and each discharging opening (103) is communicated to sedimentation volumes (324 and 424) to force the fluid flow from the inlets (301 and 401) to the sedimentation volumes (324 and 424) to flow through the channels (100); the channels (100) are vertically stacked from bottom to top, and the vertically-adjacent channels (100 a/b, b/c,..., g/h) are connected with each other through discharging holes (110) formed in partitioning walls (108) and are separated from each other in the vertical direction through the partitioning walls (108).

Description

Be used for from the dried up system of oil content

Technical field

The present invention relates to a kind of system that separates discontinuous phase for the continuous phase from emulsion, wherein discontinuous phase liquid has the proportion higher than continuous phase liquid.More particularly, the present invention relates to the system for the separation of hydrocarbons water droplet from for example fuel or oil.

Background technology

Be contained in oil, for example, water in lubricating oil, gear drive oil or hydraulic oil may seriously have influence on oily performance.Therefore need to remove water from oil.But water may fine dispersion and emulsification in oil, and exists multiple different technology to attempt to reduce the water content in oil.Therefore, be included in hydrocarbon fuel, for example, water in diesel oil, fuel oil or similar fuel may have influence on the availability of fuel.Therefore, need to reduce as much as possible the water content in such fuel.

According to a kind of technology, process fuel/oil with three steps: filtration step, it is for removing fume; Coalescent (coalescence) step, it is for being agglomerated into drop by water; And, precipitation step, wherein water droplet accumulates in bottom and the oily top that accumulates in the first continuous phase in sedimentation container top as the second continuous phase of sedimentation container as the first Continuous Liquid Phase.Then by remove at the tap of sedimentation container bottom water and can by sedimentation container top or the tap of the position, surface that is separated at least forming between the first liquid phase and second liquid phase in sedimentation container extract out oil.

First step and second step are capable of being combined in a filtration/coalescing element.For example, can comprise natural fiber for the filtration of combining and coalescent so known element, such as cellulose fibre, it is bonded together by binding agent.Filter element can be shaped in multiple favourable mode, for example, and as disclosed in US 4 549 963.For example be disclosed in US 2011/0147299 A1 for filter oil and other material of serving as coalescing medium.The background parts of US 2011/0147299 A1 is also provided for removing from oil the summary of the different technologies of water.

Conventionally, be output as from the first two step the emulsion that Water-In-Oil drips.Third step is the efficiency that the efficiency of precipitation step can limit total separation process.In the time that removal process expection is carried out with circulation style, this becomes problem especially.And in some arranges, the size that can be used for sedimentation container may be limited.Therefore be desirable to provide a kind of water scavenging system, it has improved precipitation step and compact and efficient sedimentation device is provided.

In the application's context, reference to gravitational defines term " upwards " and " downwards ", "up" and "down" and " top " and " bottom ", wherein vertical direction is defined as being parallel to gravity direction, and horizontal direction is defined as perpendicular to gravity direction.In the time mentioning slender body, term " axially " refers to direction of elongate, and term " laterally " refers to direction perpendicular to axial direction.For example, passage can be considered to elongated object, wherein, axially along passage, and is laterally the direction perpendicular to passage.Laterally therefore perpendicular to the axial leap cross section of passage.

Summary of the invention

The drop phase that the object of the present invention is to provide a kind of first liquid for separating of for example water and for example oil or mass density are lower than the system of the continuous phase of the second liquid of other hydro carbons of the mass density of water, and it can be with circulation style operation and the replacement scheme that has overcome at least some defect in the defect of above being mentioned or known method is at least provided.

According to an example, this realizes by separating first liquid and second liquid, first liquid forms the discontinuous phase of emulsion and the continuous phase of second liquid formation emulsion, and wherein first liquid has the mass density higher than second liquid, and this layout comprises the following steps:

-receive the inlet streams of emulsion in porch;

-extract the output stream of second liquid out from the top of settling volume (volume);

-make the continuous phase of first liquid accumulate in the bottom of settling volume; And

-remove first liquid from the bottom of settling volume;

Wherein, this is further comprising the steps of before being arranged in the emulsion in settling volume being processed:

-by emulsion being fed in the horizontal channel of multiple vertical stackings and inlet streams is distributed in the horizontal downwelling of multiple vertical stackings, each passage has feeding opening at entrance side place, and on the outlet side adjacent with settling volume, has exhaust openings,

-allow the drop of the first liquid in each downwelling to drop to the bottom of this downwelling, maintain simultaneously second liquid in the direction along passage the bottom horizontal flow sheet from feeding opening to exhaust openings,

-for thering is downwelling on this upper channel each who is arranged in the vertical adjacent lower channel below upper channel, the bottom of the upper downwelling from upper channel, by the unrestrained aperture in upper channel bottom, the drop of unrestrained first liquid, thus drop is injected in the lower downwelling in lower channel; And

-downwelling from horizontal channel is discharged in settling volume by exhaust openings.

By distribution entry on multiple passages stream, realize and be convenient to the flow pattern that the drop of first liquid and the continuous phase of second liquid separate.Each passage transports the downwelling of the emulsion of the drop that comprises first liquid in the continuous phase of second liquid.Because the drop of first liquid has than the higher mass density of second liquid around, the given fluid element that the downwelling in passage makes emulsion is from feeding opening in the horizontal direction in the time that exhaust openings moves forward, and drop declines gradually under the impact of gravity.Arrived behind the bottom to routing at the drop of first liquid, the permission of unrestrained aperture is in downward direction from remove these drops to routing, and the stream of second liquid is guided in the horizontal direction further along passage simultaneously.Due to the result of stacked arrangement, the drop removing from upper channel is injected in the lower channel of upper channel below, that is, in fact first liquid is added to emulsion mobile in lower channel.But, the drop of the first liquid disperseing in second liquid by combination (coalescent), drop injection causes droplet growth with the combination of the flow of confined channel.Drop in lower channel can sink to the bottom of this passage equally, and can be therefrom unrestrained and be injected into the other passage that is positioned at lower channel below, and by that analogy.Thus, in the time that emulsion is advanced to exhaust openings from feeding opening, by little by little augmenting and realized first liquid from the unrestrained first liquid of upper channel and separate with first of second liquid from the unrestrained first liquid of upper channel and to the emulsion this stacking lower channel.Meanwhile, due to the coalescent growth of drop, total droplet size also can little by little increase.Finally, flow in common settling volume at its exhaust openings emission level from stacked channels, wherein the fluid of discharge shows significant concentration gradient at vertical direction, makes compared with the top with settling volume, and the first fluid of higher concentration is injected into the bottom of settling volume.Thus, realized the efficiency that separation process improves.And, the size increasing at the drop of exhaust openings place discharge also can further improve settling volume in the efficiency of Gravity Separation.

Finally, in the time having gathered the first liquid of specified rate, make fluid separated from one another by the output stream that removes first liquid from settling volume bottom and extract second liquid from the top of settling volume out.Conventionally, extract constantly second fluid out with the speed of the local entrance flow rate of the second liquid corresponding to porch, this process can be carried out with circulation style.In certain embodiments, also may be from the bottom of settling volume unrestrained first liquid constantly.

The stacking stream distributor that is used as of horizontal channel.Preferably, passage and inlet manifold are configured to substantially on all horizontal channels, substantially distributing equably from the fluid stream of entrance reception, therefore, guarantee, in passage, all fluid elements are processed to the substantially the same time of staying, or only minimized or at least shorten at any decentralization of processing in the time of staying.

Further preferably, be greater than total lateral cross section area of the Vertical Channel of the cross-sectional area of entrance by setting, compared with inlet streams speed, for the given treating capacity of this device, the flow rate of sedimentation passage reduces.

Advantageously, according to a preferred embodiment of the invention, this device is for removing water from hydrocarbon fluid, and wherein, discontinuous phase is that water and continuous phase are hydrocarbon fluid, for example fuel or oil.

In addition, according to the device for separating of first liquid and second liquid embodiment, before this is arranged in inlet streams is distributed on the horizontal downwelling of multiple vertical stackings, also comprise make emulsion by filter medium to remove fume and/or by coalescing medium, thereby promote first liquid to gather into the step of drop.By added filtration step and/or agglomeration step before precipitation step, therefore improve separative efficiency.Filtering particles pollutant has improved droplet growth efficiency coalescent and subsequently.Make emulsion conventionally increase average droplet size or at least initial coalescent to be increased in the droplet size of transferring to the emulsion of downwelling in precipitation step as input by coalescing medium.

In addition, according to an embodiment of the layout/device for separating of first liquid and second liquid, filter medium also serves as coalescing medium.Thus, realized compactness and the high-efficient disposition for carrying out filtration and agglomeration step.The example of suitable media comprises the known filter medium that for example comprises cellulose fibre, those that for example mentioned hereinbefore.

According to a further aspect in the invention, realize object of the present invention by a kind of gravitational separation device for separating of first liquid and second liquid, first liquid forms the discontinuous phase of emulsion and the continuous phase of second liquid formation emulsion, wherein first liquid has the proportion higher than second liquid, separator comprises: shell, and it has the entrance for receiving emulsion, settling volume, outlet, it extracts second liquid out for the top from settling volume, and, waste liquid port, it is for removing the first liquid gathering from the bottom of settling volume, wherein separator comprises multiple passages, each passage extends horizontally to exhaust openings from feeding opening, wherein each in feeding opening is communicated with entrance via inlet manifold, to the fluid flow point receiving from entrance is distributed in multiple passages, wherein each in exhaust openings is led to settling volume, thereby force the fluid from entrance to settling volume to flow through passage, and wherein, passage vertically one be stacked in another top, vertically adjacent passage is connected to each other by the unrestrained aperture in partition wall middle punch, partition wall makes passage separate at vertical direction.

Pending emulsion receives in porch.From entrance, emulsion is delivered to inlet manifold, it is distributed to horizontal channel to process by inlet manifold.Preferably, inlet manifold is distributing from the fluid stream of entrance reception on all passages substantially equably.After processing in passage, discharge the fluid in in common settling volume by the exhaust openings in horizontal channel.Emulsion is being divided at least after two-phase, extract second liquid out by the outlet that is connected to settling volume top and is conventionally arranged in cover top portion, and remove second liquid by the waste liquid port that is connected to settling volume bottom and be conventionally arranged in outer casing bottom.

Inlet manifold and outlet manifold are only communicated with settling volume fluid by passage, that is, any stream that is fed into separator from entrance must be via inlet manifold by the passage of vertical stacking before arriving settling volume.Thus, introduce extra sedimentation/agglomeration step carry out actual sedimentation in settling volume before.The stacking passage of level makes flow point layer, and the aperture of connection horizontal channel allows first fluid to sink to bottom in total layering (stratify) horizontal flow of second fluid, thereby utilizes the drop of first liquid to augment the bottom of stratified flow.By unrestrained aperture, the drop of first liquid is injected in the affined horizontal flow of second liquid of the drop that transports first liquid itself, can increases droplet collision, thereby promoted the coalescent growth of first liquid drop.Stacking when mobile along horizontal channel in stratified flow, the concentration of the first liquid in the top of stratified flow reduces, and the relative concentration of first fluid in the bottom of stream increases with answering, and droplet size increases, the stacking exhaust openings in horizontal channel distributes at vertical direction, the upper channel output that makes to have lower first liquid concentration is fed directly into the top of settling volume, and the lower channel output with higher first liquid concentration is fed directly into the bottom of settling volume.Therefore the CONCENTRATION DISTRIBUTION that fills the layering of first liquid and second liquid to settling volume, wherein first liquid accumulates in bottom, and second liquid accumulates in top.Thus, improved the separative efficiency of sedimentation device.

Advantageously, according to an embodiment, passage stacks as high is mated settling volume height substantially to improve the transfer/injection of the layering CONCENTRATION DISTRIBUTION from horizontal channel to settling volume.

From channel size and total number of channels, can determine the total sectional area of the passage in stacking.Preferably, total sectional area is greater than entrance section, to reduce the flowing velocity of distributed flow in horizontal channel.Therefore, for given entrance flow rate, increased the mean residence time for the treatment of the fluid element of emulsion in separator, because increased the cumulative volume of gravitational separation device.

Determined the average treatment amount of separator by the average inlet flow rate of given period.The mean residence time of processing fluid element by separator can be determined to be in the average flow scale of construction that exists in the given period separator average inlet flow rate divided by this period.For given nominal/average inlet flow rate, the upper limit of mean residence time can be estimated as to the internal volume of the separator that can be used for liquid divided by nominal/average inlet flow rate.

According to an embodiment, horizontal channel can comprise many group passages, and every group forms the independent vertical stacking that is independent of one or more other vertical stacking horizontal channel group work.

Advantageously, according to an embodiment, the quantity that is stacked on the passage in top of each other is at least 5, alternatively at least or about 10, and alternatively at least or about 15, alternatively at least or about 20, or about 25.Increase number of channels and improved layered effect.On the other hand, the channel cross-section reducing causes the flow resistance increasing.For given stacks as high, can should not exceed from the pressure drop at separator two ends the condition derivation of predetermined design specification for the favourable upper limit of number of channels.

In addition, according to separator embodiment, inlet manifold is the center cavity/endoporus vertically extending, passage extends to the exhaust openings at settling volume place on outward direction around the feeding opening at the inlet manifold place, center cavity/arrangement of bores Yi Cong center of vertical extension, settling volume is arranged in around passage.Settling volume also serves as the outlet manifold of collecting from the downwelling of all horizontal channels output.Advantageously, the inwall of shell limits the external boundary of settling volume, and the stacking external envelope of passage limits the inner boundary of settling volume.In addition advantageously, shell has the circular cross-section in horizontal plane.

In addition, according to separator embodiment, passage is around central inlet manifold spiral winding.By making passage around inlet manifold spiral, wherein feeding opening in center and exhaust openings around, realized compact device.For the stacking given outside dimension of passage, increase passage length.

In addition, according to separator embodiment, the spiral number of turn of passage is at least 2, preferably at least 3, alternatively at least 4 or at least 5.For given nominal entrance flow rate, do not reduce channel cross-section by increasing passage length, increase the time of staying, thereby improved separative efficiency.The flow resistance that the passage length increasing causes passage to increase.The upper limit of passage length can be determined according to the predeterminated target of the maximum acceptable pressure drop in separator two ends in the circulation operation of measuring from the inlet to the outlet again.Advantageously, according to an embodiment, passage length is at least 0.5 m; At least 1 m; Or at least 2 m.

In addition, according to separator embodiment, each passage has certain lateral cross section area, has at the channel height of horizontal vertical direction with at the channel width of transverse horizontal direction, wherein channel height is at least 1 mm, at least 2 mm, at least 5 mm, or at least 10 mm, and preferably, be less than 20 mm, or be less than 15 mm and/or wherein, channel width is at least 1 mm, at least 2 mm, at least 5 mm, or at least 10 mm, and preferably, be less than 40 mm, or be less than 30 mm, or be less than 20 mm, or be less than 15 mm.Favourable channel height can be at least or about 1 mm, 2 mm, 3 mm, 4 mm, 5 mm, 6 mm, 7 mm, 8 mm, 9 mm or 10 mm.Favourable channel height is preferably less than or about 40 mm, 30 mm, 20 mm or 15mm.Favourable channel width can be at least or about 1 mm, 2 mm, 3 mm, 4 mm, 5 mm, 6 mm, 7 mm, 8 mm, 9 mm or 10 mm.Favourable channel height is preferably less than or about 40 mm, 30 mm, 20 mm or 15mm.

In addition, according to separator embodiment, the unrestrained aperture that connects upper channel and vertical adjacent lower channel possesses from the upstream edge in aperture or is at least projected into the collar in lower channel downwards from the upstream edge in aperture.Immediately following protuberance, the collar guides to drop the bottom of the downwelling in the lower channel that they are injected into more quickly, and has promoted droplet growth by combination drop.The collar should be sized to incomplete blocks flow, that is, the long-pending sectional area that must be less than its lower channel stretching into of the projecting section of sleeve pipe, as found out in the lateral cross section of lower channel.Preferably, the projection lateral cross section area of the collar be less than the sectional area of its passage stretching into or for the sectional area of its passage stretching into about 50%.Preferably, the height of the collar is less than the height of its passage stretching into.At at least one, preferably all passages or substantially all in passages at least some, preferably whole unrestrained apertures or substantially whole unrestrained apertures can possess such collar.

Advantageously, sizing is carried out according to the minimum droplet size of predetermined nominal in unrestrained aperture.Generally speaking, minimum orifice size should corresponding to or exceed the minimum droplet size of predetermined nominal.Conventionally, passage laterally in aperture width in this direction described channel width 50% and 100% between.

Advantageously, according to an embodiment, aperture width, the port size of watching in the transverse horizontal direction of passage is less than channel width, and the minimum droplet size of at least about predetermined nominal, for example, large approximate number millimeter, for example at least or about 1 mm, alternatively at least or about 2 mm, alternatively at least or about 3 mm.Advantageously, according to another embodiment, aperture length, as along channel axis to the port size axially watching, be minimum droplet size, for example large approximate number millimeter of at least about predetermined nominal, at least or about 1 mm, alternatively at least or about 2 mm, alternatively at least or about 3 mm.Preferred orifice shapes is axially elongated passage, that is, aperture length is greater than aperture width, for example, be at least 1.2 times, at least 1.5 times or about 2 times of aperture width.

Advantageously, according to an embodiment, in passage, the gross area in unrestrained aperture is less than 50%, 40%, 30%, 20%, 10%, 5% or 2% of the total vertical projection area being covered by passage.Advantageously, according to an embodiment again, the orifice number of each passage can be at least or about 2,5,10,20 or 50.Compared with giving the gross area of routing and/or the aperture sum of each passage, the percentage of the gross area in unrestrained aperture should be configured to, to maintain the layering horizontal flow of second liquid, provide sufficient area to sink and unrestrained first liquid by aperture simultaneously.

In addition, according to separator embodiment, passage is set to be positioned over the plug-in unit of shell inner side, plug-in unit is formed as the stacking of channel plate, each channel plate comprises for making the vertically adjacent separate horizontal subdivision wall of passage, each channel plate also comprises the vertically outstanding sidewall of the passage that is limited to horizontal direction, and wherein, unrestrained aperture is arranged in horizontal subdivision wall between sidewall.Thus, in the stacking shell that is readily integrated into separator of passage.Stacking plate configuration is easy to assembling, thereby has reduced production cost.If need any inspection or maintenance, stacking also can being easy to dismantled again.

In addition, according to separator embodiment, this separator also comprises: filter and/or coalescent level, it is arranged in shell inner side between shell entrance and inlet manifold.By three levels are arranged in same shell, realize compact separator, wherein in same device, in level subsequently, carry out nearly three steps: filtration grade, coalescent level and sedimentation level.Separator shell always comprises sedimentation level, and sedimentation level has inlet manifold, settling volume and extends to the horizontal channel of settling volume from inlet manifold.Filtration grade and/or coalescent level are arranged between shell entrance and inlet manifold to forced the working fluid receiving from entrance by filtration grade and/or coalescent level before emulsion is fed into horizontal channel via inlet manifold.Preferably, these grades combine the inlet streams of emulsion that makes to receive in porch and are filtered and/or stand and and then emulsion is fed into inlet manifold after the first agglomeration step in shell.Separator shell comprises in the embodiment of filtration grade and coalescent level therein, filtration grade and coalescent level can be advantageously in single filtration plug-in unit with both kept particle contamination here and also promoted the coalescent medium of the first liquid cellulosic material of water in oil emulsion (for example for) combination.Otherwise filtration grade and coalescent level can be independent.Under latter event, coalescent level is arranged in the downstream of filtration grade, as watched on the flow direction from entrance to inlet manifold.

As mentioned above, filtering particles pollutant has improved the coalescent and efficiency of droplet growth subsequently.And, by making emulsion carry out agglomeration step before being delivered to the horizontal channel of sedimentation level, start coalescent and be conventionally increased in the drop of the first liquid in emulsion.Therefore, promoted separating of two kinds of liquid in the coalescent and sedimentation level of the drop of first liquid subsequently.This combination by given filtration grade and/or coalescent level with sedimentation level, can realize the improved settling efficiency of separator.

Brief description of the drawings

Hereinafter, further explained the present invention with reference to illustrative embodiments.Accompanying drawing shows:

Fig. 1 schematically shows according to the top view of the helical duct of an embodiment,

Fig. 2 schematically shows the sectional view stacking according to the helical duct of Fig. 1,

Fig. 3 schematically shows according to the side view of the broken section of the gravitational separation device of an embodiment,

Fig. 4 shows according to the sectional view of the partial component of the separator of another embodiment; And

Fig. 5 shows the diagrammatic view for separating of the execution step of the device of first liquid and second liquid according to an embodiment.

Reference numeral

A first liquid

B second liquid

E emulsion

A, b, c, stacking sequence number

100 horizontal channels

101 feeding openings

102,202 center gap/endoporus

103 exhaust openings

104,204 ambient surface

105 channel plates

106 grooves

107 sidewalls

108 horizontal subdivision walls

110 apertures

111 collars

200 vertical stackings

300 shells

301,401 entrances

Housing department on 310,410

311,411 filtrations/coalescing element

312,412 ambient surface

313,413 central bore

Volume around 314,414

320,420 lower casing portions

324,424 settling volumes

330,430 waste liquid ports

331,431 outlets

350,450 center assembling axles

402 cages

403 demarcation strips

404 recesses

500 processes

501 inputs

510 first order

511 filtration steps

512 agglomeration step

520 second level

521 horizontal flow stratification step

522 precipitation steps

530 waste liquids

531 outputs.

Detailed description of the invention

Fig. 1 shows the top view of horizontal channel 100.Fig. 2 shows the vertical stacking 200 of the horizontal channel 100 of being watched along the line II-II in Fig. 1 with side cross-sectional view.With reference to figure 1 and Fig. 2, the exhaust openings 103 at 104 places around path 10 0 extends to from the feeding opening 101 in center gap 102.Center gap 102 forms stacking 200 central bore 202, and central bore 202 is served as the inlet manifold for the feeding opening 101 feeding stacked channels 100 from stacked channels 100.The surrounding 104 of path 10 0 forms the ambient surface 204 of vertical stacking 200.Path 10 0 around center gap 102 with spiral three circles.But, according to the width of the diameter of the length of desirable path 10 0, center gap 102, passage, i.e. its size in transverse horizontal direction and/or any constraint for diameter around vertical stacking 200, can be susceptible to any integer or the non-integral number of turn that are greater than a circle.

Advantageously, the vertical stacking 200 that forms path 10 0 in Fig. 2 by stacking multiple level boards 105 (sorting with a-h), level board 105 comprises the groove 106 being limited by the sidewall 107 projecting upwards and/or on the bottom side of plate 105, comprises the corresponding groove (not shown) being limited by the sidewall of giving prominence to downwards on top side.Plate 105 (a – h) respectively has a center gap 102, center gap 102 the level board 105 of vertically aiming at (a – h) in the central bore 202 of formation vertical stacking 200.Vertically adjacency channel is by connecting in the unrestrained aperture 110 of partition wall 108 middle punches, and partition wall 108 makes by vertical adjacent panels 105 (a/b, b/c ..., g/h) form vertical adjacent path 10 0 separate at vertical direction.Unrestrained aperture 110 in partition wall 108 can possess from corresponding upper channel 105 (a, c ..., bottom h) is projected into vertically adjacent lower channel 100 (b, c downwards ..., h) the interior collar 111.

Fig. 3 schematically shows according to the side cross-sectional view of the gravitational separation device of an embodiment and possesses as hereinbefore with reference to figure 1 and the described stacking channel card of Fig. 2.With reference to figure 3, the vertical stacking 200 of horizontal channel 100 can be used as flow point layer interposer lies and is placed in shell 300 inner sides, thereby receives emulsion (E) stream at entrance 301 places.The emulsion (E) of locating to receive at entrance (301) comprises that wherein first fluid (A) has than the higher proportion of second liquid (B) as the first fluid (A) of the discontinuous phase of emulsion with as the second fluid (B) of the continuous phase of emulsion (E).In shell 300 inner sides, process emulsion (E) to separate first liquid (A) and second liquid (B), first liquid (A) can be removed by waste liquid port 330, and second liquid (B) can be extracted out by outlet 331.Preferably, second liquid (B) is extracted out with Continuous Flow, and separator can be operated with circulation style.The emulsion (E) receiving at entrance 301 places also can comprise pollutant, the small-particle for example disperseing in emulsion (E).Therefore can advantageously comprise the first order of band filtration and/or coalescing element 311 for separating of first liquid (A) and the device of second liquid (B), before carrying out Gravity Separation at second level convection cell (A, B), keep such pollutant here.

Advantageously, the top 310 that filtration/coalescing element 311 is positioned over shell 300 neutralizes the upstream of the flow point layer plug-in unit being formed by the vertical stacking 200 of horizontal channel 100.Entrance 301 is positioned over the upstream of filtration/coalescing element 311, be defined in the inner side of housing department 310 and filtration/coalescing element 311 around in the top 310 of the shell 300 that is communicated with of surrounding's volume 314 fluids between input side 312.Around volume 314 around filtration/coalescing element 311 on whole input side 312 distribution entry stream.Filtration/coalescing element 311 is configured to receive input fluid from input side 312 around, process fluid to keep drop coalescent of pollutant and/or beginning/stimulation first liquid (A) here in filter, and filter liquor is discharged into central bore 313, and wherein the filter liquor on the outlet side of filtration/coalescing element is also usually included in the drop (A) disperseing in continuous phase (B).

Gravity Separation level is positioned in the bottom 320 of shell 300.The settling volume 324 that the surrounding of the sheath between 320 inner sides, bottom that Gravity Separation level comprises the flow point layer plug-in unit being formed by the vertical stacking 200 of horizontal channel 100 and is defined as shell 300 and stacking 200 the surrounding of passage around passage stacking 200 arranges.The settling volume 324 that surrounding's volume 314 of upper housing department 310 and the surrounding of lower casing portion 320 arrange is separated from one another, and top 310 is only communicated with bottom 320 by central bore 313,202, and central bore 313,202 is relative to each other placed to and axially aligns.Therefore pending emulsion (E) stream enters shell 300 from entrance 301; Flow through by volume 314 around and be delivered to by filtration/coalescing element 311 in the central bore 313 of filtration/coalescing element 311.From the central bore 313 of filtration/coalescing element 311, circulation moves on to the central bore 202 of the vertical stacking 200 of horizontal channel 100.Central bore 202 is served as inlet manifold with 101 while of the corresponding feeding opening feeding horizontal channel concurrently by passage.In the inner side of passage stacking 200, stream is layered as by the horizontal subflow of the second fluid of respective horizontal path 10 0 (B), and allows the drop of first liquid (A) to decline towards stacking bottom by being arranged at the unrestrained aperture 110 between vertical adjacency channel.Therefore around vertical stacking 200 204 discharge horizontal subflow in the vertical directions there is concentration gradient, wherein the first fluid of higher concentration (A) at lower area and the first fluid (A) of corresponding low concentration in upper area.Therefore, first fluid (A) accumulates in the bottom of settling volume 324, and it can remove by waste liquid port 330 therefrom.Second fluid (B) accumulates in the top of first fluid (A) in settling volume 324 tops, and it can be extracted out by outlet 331 therefrom.Total assembly is tightened and is kept together by central shaft 350.

Fig. 4 shows according to the present invention expection for from oil (continuous phase, second liquid) Separation of Water (decentralized photo, first liquid) the vertical section figure of partial component of another embodiment of device, wherein the lid of cover top portion 410 removes from its seat 402.Surrounding's volume 414 that entrance 401 is arranged in the top 410 of shell and limits with the ambient surface 412 of inner surface by upper housing department 410 (comprising the lid removing) and filtration/coalescing element 411 is communicated with.The fluid receiving from entrance is distributed in ambient surface 412 and by filtration/coalescing element 411 via volume 414 around.The filter liquor that is included in the drop of the first liquid disperseing in second liquid receives in central bore 413, central bore 413 is with vertically assembling axle 450 is coaxial, and in the direction of vertical assembling axle 450 axially transferring to the Gravity Separation level being arranged in outer casing bottom 420.Settling volume 424 is formed on the bottom of shell 420, and it comprises the oil export 431 that is connected to settling volume 424 upper areas, and is used for the waste liquid port 430 of water in the bottom of settling volume 424.Around in cover top portion 410, volume 414 and the settling volume in bottom 420 424 are by being held on demarcation strip 403 on recess 404 and separated from one another.Filtration/coalescing element 411 is arranged in the top of separating plate 403 and is only communicated with the bottom 420 of shell by central bore 413 and the corresponding center gap in demarcation strip 403.The vertical stacking 200 of horizontal channel 100 hangs to extend in settling volume from demarcation strip 403.Horizontal channel 100 is around central bore 202 spirals of vertical stacking 200.The central bore 202 of vertical stacking 200 and the central bore 413 of filtration/coalescing element 411 are axially aligning and at sealed bottom.Therefore the fluid that central bore 413 is transferred to the lower central bore 202 of vertical stacking 200 from filtration/coalescing element 411 is forced through horizontal channel 100 arriving before settling volume 424.Water (first liquid) accumulates in settling volume bottom and can remove by waste liquid port 430.Oil (second fluid) accumulates in the top of water and can extract out by outlet 431, preferably mobile to operate separator with circulation style to continue.

Fig. 5 shows the figure that uses process according to an embodiment of the invention oil that emulsion (E) is for example polluted by water to process.Process 500 comprises the input 501 of the first liquid (A) that receives the discontinuous phase in the continuous phase that emulsification is second liquid (B), and wherein first liquid (A) has higher relative density compared with second liquid (B).Can comprise other pollutant, for example fume as input 501 received emulsions (E).Advantageously, therefore, in the first order 510, emulsion is by filtration step 511, to remove such fume.At agglomeration step 512 places, stimulate the coalescent of the discontinuous phase that formed by first liquid (A), for example, by interacting with coalescing medium.In advantageous embodiment, in same filtration/coalescing element, carry out filtration step 511 and agglomeration step 512, wherein the material of element serves as filter medium and promotes the coalescent coalescing medium of first liquid (A).In the first order 510, after coalescent 512, the drop of first liquid (A) disperses in second liquid (B).Then pretreated like this emulsion is delivered to the second level 520 from the first order 510, carries out A/W in the second level 520 and separate.The second level 520 comprises stream stratification step 521, wherein the inlet streams of the emulsion here receiving via the first order 510 is distributed on the horizontal channel of multiple vertical stackings and makes flow point layer.Passage is configured to maintain the equally distributed horizontal flow substantially of second fluid (B), and make vertical adjacency channel unrestrained hole connected to one another allow discontinuous phase (first liquid, A) drop declines towards the bottom of the stratified flow of continuous phase (second liquid, B) by unrestrained hole under weight-driven.In the time that it declines, other drop combination of the drop of first liquid (A) and first liquid (A), and therefore size increases.Precipitation step subsequently 522 in settling volume, first liquid (A) is last as gathering mutually separately in second liquid (B) below, the output 531 of second liquid (B) can be extracted out from the settling volume top of the top, interface that is separated between first liquid and second liquid, and the waste liquid 530 of first liquid (A) can be from the bottom discharge of settling volume.

Claims (9)

1. the gravitational separation device for separating of first liquid (A) and second liquid (B), described first liquid (A) forms the continuous phase of discontinuous phase and described second liquid (B) formation emulsion (E), wherein, described first liquid (A) has than the higher mass density of described second liquid (B), described separator comprises: shell (300), it has the entrance (301,401) for receiving described emulsion (E), settling volume (324,424), outlet (331,431), it is for extracting described second liquid (B) out from the top of described settling volume (324,424), and, waste liquid port (330, 430), it is for from described settling volume (324, 424) bottom removes the first liquid (A) gathering, it is characterized in that, described separator comprises multiple passages (100), each passage (100) extends horizontally to exhaust openings (103) from feeding opening (101), wherein, each in described feeding opening (101) is via inlet manifold (202) and described entrance (301, 401) be communicated with, so that will be from described entrance (301, 401) the fluid flow point receiving is distributed in described multiple passage (100), wherein, each in described exhaust openings (103) is led to described settling volume (324, 424), thereby force fluid from described entrance (301, 401) flow to described settling volume (324, 424) to pass through described passage (100), and wherein, described passage (100) vertically one be stacked in another top, vertically adjacent passage (100 a/b, b/c, g/h) by being connected to each other in the unrestrained aperture (110) of partition wall (108) middle punch, described partition wall (108) makes described vertically adjacent passage (100 a/b, b/c, g/h) in the vertical direction is separate.

2. separator according to claim 1, it is characterized in that, described inlet manifold (202) is the center cavity/endoporus vertically extending, described passage (100) extends at described settling volume (324 at outward direction with the feeding opening (101) from described central inlet manifold (202) around the center cavity/arrangement of bores of described vertical extension, 424) exhaust openings (103) of locating, described settling volume (324,424) is arranged in described passage (100) around.

3. separator according to claim 2, is characterized in that, described passage (100) is around described central inlet manifold (202) spiral winding.

4. separator according to claim 3, is characterized in that, the spiral number of turn of described passage (100) is at least 2, preferably at least 3, alternatively at least 4 or at least 5.

5. according to the separator described in any one in aforementioned claim, each passage (100) has certain lateral cross section area, wherein, the horizontal vertical direction in channel height edge and channel width are along transverse horizontal direction, wherein, described channel height is at least 1 mm, at least 2 mm, at least 5 mm, or at least 10 mm, and preferably, be less than 20 mm, or be less than 15 mm, and/or, wherein, described channel width is at least 1 mm, at least 2 mm, at least 5 mm, or at least 10 mm, and preferably, be less than 40 mm, 30 mm, 20 mm, or be less than 15 mm.

6. according to the separator described in any one in claim 1-4, it is characterized in that, connect upper channel (100 a, b,, g) with vertical adjacent lower channel (100 b, c, h) unrestrained aperture (110) possesses the collar (111), and the described collar (111) is projected into described lower channel (100 b, c downwards from least upstream edge of described aperture (110),, h) in.

7. according to the separator described in any one in claim 1-4, it is characterized in that, described passage (100) is set to be positioned over the plug-in unit (200) of described shell (300) inner side, described plug-in unit is formed as the stacking of channel plate (105), each channel plate (105) comprises for making vertically adjacent passage (100 a/b, b/c, g/h) separate horizontal subdivision wall (108), each channel plate (105) also comprises the vertical outstanding sidewall (107) of the described passage (100) for being limited to described horizontal direction, wherein, described unrestrained aperture (110) is arranged at described in described horizontal subdivision wall (108) between sidewall (107).

8. according to the separator described in any one in claim 1-4, it is characterized in that, described separating device also comprises and is arranged in the entrance (301 of described shell inner side at described shell (300), 401) filtration and between described inlet manifold (202) and/or coalescent level (311,411).

9. separator according to claim 8, is characterized in that, described filter medium also serves as coalescing medium.