CA1083012A - Process and apparatus for achieving a uniform flow profile - Google Patents
Process and apparatus for achieving a uniform flow profileInfo
- Publication number
- CA1083012A CA1083012A CA247,615A CA247615A CA1083012A CA 1083012 A CA1083012 A CA 1083012A CA 247615 A CA247615 A CA 247615A CA 1083012 A CA1083012 A CA 1083012A
- Authority
- CA
- Canada
- Prior art keywords
- flow
- tube
- bands
- disc
- outs
- Prior art date
- Legal status (The legal status is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the status listed.)
- Expired
Links
Classifications
-
- F—MECHANICAL ENGINEERING; LIGHTING; HEATING; WEAPONS; BLASTING
- F15—FLUID-PRESSURE ACTUATORS; HYDRAULICS OR PNEUMATICS IN GENERAL
- F15D—FLUID DYNAMICS, i.e. METHODS OR MEANS FOR INFLUENCING THE FLOW OF GASES OR LIQUIDS
- F15D1/00—Influencing flow of fluids
- F15D1/02—Influencing flow of fluids in pipes or conduits
Landscapes
- Engineering & Computer Science (AREA)
- Physics & Mathematics (AREA)
- Fluid Mechanics (AREA)
- Mechanical Engineering (AREA)
- General Engineering & Computer Science (AREA)
- Physical Or Chemical Processes And Apparatus (AREA)
Abstract
ABSTRACT OF THE DISCLOSURE:
A process and apparatus for achieving a uniform flow profile of very viscous liquids when flowing through a tube or reaction chamber. The very viscous liquid is passed through at least two sets of annular spaces arranged at axial intervals within the tube or reaction chamber, the annular spaces of each set extending concentrically with increasing diameter over the entire cross-section of the tube or reaction chamber and having the same depth in the direction of flow, the annular spaces of two consecutive sets being staggered with respect to each other as viewed in the direction of flow. The apparatus of the invention consists of a combination of two or more discs arranged at axial intervals within a tube transversely to the direction of flow, each disc consisting of a plurality of ring-shaped bands of increasing diameter, the bands being arranged freely of one another and concentrically at intervals on a grid supporting means to provide correspondingly concentric open spaces between the bands over the entire cross-section of the tube, with the walls of the bands running parallel to the direction of flow, and the bands of the separate discs being staggered with respect to each other as viewed in the direction of flow.
A process and apparatus for achieving a uniform flow profile of very viscous liquids when flowing through a tube or reaction chamber. The very viscous liquid is passed through at least two sets of annular spaces arranged at axial intervals within the tube or reaction chamber, the annular spaces of each set extending concentrically with increasing diameter over the entire cross-section of the tube or reaction chamber and having the same depth in the direction of flow, the annular spaces of two consecutive sets being staggered with respect to each other as viewed in the direction of flow. The apparatus of the invention consists of a combination of two or more discs arranged at axial intervals within a tube transversely to the direction of flow, each disc consisting of a plurality of ring-shaped bands of increasing diameter, the bands being arranged freely of one another and concentrically at intervals on a grid supporting means to provide correspondingly concentric open spaces between the bands over the entire cross-section of the tube, with the walls of the bands running parallel to the direction of flow, and the bands of the separate discs being staggered with respect to each other as viewed in the direction of flow.
Description
108;3~1~
The present inventiorl ~o:latec; t~ a p~oce~s and apparatus for achieving ~ uniform flow proEile of very viscous li-~uids when flowing through tubes or reactiorl chambers.
When fluicls of hiyh viscosity fLow through tubo~ or reaction chambers it is difficult to achieve a uniform flow profile, that is to say a uniform rate of flow over the entire cross-section.
The effect of the wall on the flow is that the central part of the viscous fluid flows faster. As a consequence, the residence time of individual portions of the fluid in the tube or reaction chamber differs and a large proportion of the fluid only leaves the tube or the reaction chamber after a longer time than -the parts of the fluid which are in the middle zone. This is un-desirable if a reaction takes place in the fluid and its progress , depends on the residence time. Particularly in the case of poly-merization reactions or polycondensation reactions, e.g. in the case of the manufactùre of polycaprolactam, a variable residence ti.me results in a substantially broader spectrum of constituents of higher molecular weight and lower molecular weight.
' German Patent 1,136,310 discloses a device for j~ 20 achieving a uniorm flow profile, wherein cylindrical packings,held , together in a hexagonal arrangement to form discs, are provided with inward-projecting wall cut-outs and the discs are fitted at inter-valsj at right angles to the direction of flow, into the tube or reaction chamber through which the fluid flows. However, the . , ~
manufacture o~ such discs is technically very complicated since :.
~- it is necessary first to manufacture the individual cylindrical , packings and then to join together a plurality of these packings.
In addition, the device has the disadvantage that once the order of magnitude oE the packings has been decided on, it can only be changed by replacing all the packings. Finally, this prior art ; device has the disadvantage that the open spaces are not uniform ;~ as dead spaces remain between the individual packings.
, . ...
., ~, - 1 -.'' , ' .
, .~ . .
,:' , , ' L~
~ e obj~ci oE l~i.s ~ verl~:iorl is to ~,rc>v:i~c~ a L~rofess whlch ac~-lleves cl ul~iEorm flc)w:in hicJh.l~ viscous ~i.qll:i(1c,. It i5 another objcct of tlle :invenl:iorl to prov:ide oE)en sp;lceC; ~J~IiCil are un:i.Eo~m over the enti.re cross-secL:iorl oE ttle 1OW tube or reactior chamber. Yet ano~her object o:E the invention is to ensure that no dead spaces are formed. Finally, it is an object of the invention to provide a suitab].e apparatus therefor.
In aceordance with this invention, these and other objects are achieved in a process fo:r obta:ining a uniform flow profile of very viscous liquids when :Elowing through a tube or reaction chamber, wherein the very viscous liquid is passed through at least two sets of annular spaees arranged at axial intervals within the tube or reac-tion chamber, the annular spaees of eaeh set extending eoneen-trieally with inereasing diameter over the -. en-tire eross-seetion of the tube or reaetion ehamber and having the same dep-th in the direetion of flow, the annular spaees of two eonseeutive se-ts being staggered wi-th respee-t to eaeh other as viewed in the direetion of flow.
The proeess aeeording to the invention is aehieved by means of an apparatus for obtaining a uniform flow profile of a highly viseous liquid when flowing through a tube, and eonsisting . of a combination of two or more dises arranged at axial intervals -; within said tube transversely to -the direction of flow, each disc , eonsisting of a plurality of ring-shaped bands of inereasing diameter, the bands being arranged freely of one another and ; eoneentrieally at intervals on a grid supporting means to provide eorrespondingly eoneentrie open spaees between the bands over the en-tire eross-sec-tion o:E the tube, with the walls of -the bands running parallel to the direetion of flow, and the bands of the ~ ~
.. 30 separate dises being staggered with respeet to each o-ther as :~ :.
I viewed in the direction of flow.
Preferred very viscous fluids are, e.g., polylae-tam melts which are ob-tainecl on polycondensation of laetams of 5 to 13 ring members of from 1~0 to 250C. The proeess and the apparatus
The present inventiorl ~o:latec; t~ a p~oce~s and apparatus for achieving ~ uniform flow proEile of very viscous li-~uids when flowing through tubes or reactiorl chambers.
When fluicls of hiyh viscosity fLow through tubo~ or reaction chambers it is difficult to achieve a uniform flow profile, that is to say a uniform rate of flow over the entire cross-section.
The effect of the wall on the flow is that the central part of the viscous fluid flows faster. As a consequence, the residence time of individual portions of the fluid in the tube or reaction chamber differs and a large proportion of the fluid only leaves the tube or the reaction chamber after a longer time than -the parts of the fluid which are in the middle zone. This is un-desirable if a reaction takes place in the fluid and its progress , depends on the residence time. Particularly in the case of poly-merization reactions or polycondensation reactions, e.g. in the case of the manufactùre of polycaprolactam, a variable residence ti.me results in a substantially broader spectrum of constituents of higher molecular weight and lower molecular weight.
' German Patent 1,136,310 discloses a device for j~ 20 achieving a uniorm flow profile, wherein cylindrical packings,held , together in a hexagonal arrangement to form discs, are provided with inward-projecting wall cut-outs and the discs are fitted at inter-valsj at right angles to the direction of flow, into the tube or reaction chamber through which the fluid flows. However, the . , ~
manufacture o~ such discs is technically very complicated since :.
~- it is necessary first to manufacture the individual cylindrical , packings and then to join together a plurality of these packings.
In addition, the device has the disadvantage that once the order of magnitude oE the packings has been decided on, it can only be changed by replacing all the packings. Finally, this prior art ; device has the disadvantage that the open spaces are not uniform ;~ as dead spaces remain between the individual packings.
, . ...
., ~, - 1 -.'' , ' .
, .~ . .
,:' , , ' L~
~ e obj~ci oE l~i.s ~ verl~:iorl is to ~,rc>v:i~c~ a L~rofess whlch ac~-lleves cl ul~iEorm flc)w:in hicJh.l~ viscous ~i.qll:i(1c,. It i5 another objcct of tlle :invenl:iorl to prov:ide oE)en sp;lceC; ~J~IiCil are un:i.Eo~m over the enti.re cross-secL:iorl oE ttle 1OW tube or reactior chamber. Yet ano~her object o:E the invention is to ensure that no dead spaces are formed. Finally, it is an object of the invention to provide a suitab].e apparatus therefor.
In aceordance with this invention, these and other objects are achieved in a process fo:r obta:ining a uniform flow profile of very viscous liquids when :Elowing through a tube or reaction chamber, wherein the very viscous liquid is passed through at least two sets of annular spaees arranged at axial intervals within the tube or reac-tion chamber, the annular spaees of eaeh set extending eoneen-trieally with inereasing diameter over the -. en-tire eross-seetion of the tube or reaetion ehamber and having the same dep-th in the direetion of flow, the annular spaees of two eonseeutive se-ts being staggered wi-th respee-t to eaeh other as viewed in the direetion of flow.
The proeess aeeording to the invention is aehieved by means of an apparatus for obtaining a uniform flow profile of a highly viseous liquid when flowing through a tube, and eonsisting . of a combination of two or more dises arranged at axial intervals -; within said tube transversely to -the direction of flow, each disc , eonsisting of a plurality of ring-shaped bands of inereasing diameter, the bands being arranged freely of one another and ; eoneentrieally at intervals on a grid supporting means to provide eorrespondingly eoneentrie open spaees between the bands over the en-tire eross-sec-tion o:E the tube, with the walls of -the bands running parallel to the direetion of flow, and the bands of the ~ ~
.. 30 separate dises being staggered with respeet to each o-ther as :~ :.
I viewed in the direction of flow.
Preferred very viscous fluids are, e.g., polylae-tam melts which are ob-tainecl on polycondensation of laetams of 5 to 13 ring members of from 1~0 to 250C. The proeess and the apparatus
- 2 -: ~ . , . - . : .
: . :
'; . ' ' ' ' , '
: . :
'; . ' ' ' ' , '
3~
are o~ particul~r industrial impo~tance in connection ~Jith the manu~acture o~ polycaprolactam.
n accord~nce with the inverltion, the ver~ viscous li~uid ls passed through annular spaces. l'he width of the spaces is advantageously ~rom 1.75 to 5 cm. The spaces extend concentrically with increasing diame-ter over the entire cross-seetion o~ the tube or reaction cham~er. The term "concentrically" means that the distanee b~-tween any one annular space and -the axis of the tube or reaction ehamber is the same at all points, and the distanee between any one annular spaee and the walls of the tube or reaction chamber is the same at all points. The annular spaees - are formed by eoneentrieally arranged ring-shaped bands of inereasing diameter. The width of all the bands of any one dise is the same. The walls of the ring-shaped bands run parallel to the `~ direction of ~low of the very viscous liquid and eonsequently parallel to the walls of the tube or reaction chamber. In aeeordanee with the invention, the annular spaees have the same ; depth in the direetion of flow and run parallel, as viewed in the direetion of flow. As the very viseous liquid flows through the tube or reaetion chamber, it is passed -twiee or more times through annular spaces extending eoneentrically with inereasing diameter over the entire eross-section of the tube or reaetion chamber, the seeond and subsequent annular spaees being staggered with - respeet to the preeeding annular spaee. The depth of the annular spaees in the direetion of flow is advantageously from 1.5 to 10, espeeially 3.5 to 8, em. Once the depth has been seleeted, it remains the same for all the annular spaees of a dise over the entire cross-seetion of the tube or reaetion ehamber. As a rule, the width of the annular spaees, i.e., the distanee between the bands, is eonstant over the entire eross-seetion of the tube or reaetion ehamber. However, it is also possible for the width of the annular spaees to increase or deerease with inereasing diameter ~ 3 ~
.
1~3~
so as to counterbalarlc~ a chancJe in the flow charact~risticc.
of 'che melt, as may arisc, ~or inst:ance, through additional int~rnal or ex~ernal heatincJ.
The very viscous 1iquld flows at least twice~ through concentric annular spaces extending over the entire cross-section of the tube or reaction chamber. The annular spaces are advan-tageously from 3.5 to 20 cm apart, in -the direction of flow. It has proved to be particularly aclvantayeous to pass the highly viscous melt through annular spaces from 4 -to lO times per meter of reaction chamber.
The new apparatus comprises two or more discs arranged at axial intervals within a tube or reactlon chamber transversely to the direction of flow~ ~dvantageously, the dis-tance, in the direction of flow, between the discs is from 3.5 to 20 cm. It has ~-~ proved advantageous to use from 4 to 10 discs per meter length, in reaction chambers. In another advantageous embodiment, the discs are solely separated from one another by the support structure (described in more detail below) which serves as a spacer.
In a vertical reaction chamber, therefore, only the support , structure of the bottom disc is attached to the walls of the chamber, or simply placed on an annular bead in the wall of the ` tube or reaction chamber, and the remaining discs with their , support structures are placed on top.
~ Each disc consists of a plurality of ring-shaped bands ; of increasing diameter, the bands being arranged freely of one another and concentrically at intervals on a grid supporting means.
The ring-shaped bands are preferably from 1.5 to lO cm wide, and especially from 3.5 to 8 cm wide. The distance between the indi-vidual ring-shaped bands is advantageously from 1.75 to 5 cm. As a rule, the distances between the individual ring-shaped bands are constant. However, it is also possible to arrange the ring-shaped bands, of increasing diameter, at larger or smaller distances so .:
' . ~ , -~0~3~
as to counterbalance a challcJe in ~he flow characteristics of the melt, as may arisc, e.g., throucJh additional in~ernal or e~ternal heating. In order ~o prevent thc vi~cous eluid in the center oE
the disc from moving Easter, a displacer body is advantageou51y provided there, -the body preferably haviny conical ends.
To prevent the concentrically arranged bands from moving, they are attached, e.g., by welding, to a grid-like support. The support is for example a wide-meshed grid consistiny of profiles, or a sheet metal grid, the walls of which run parallel to the direction of flow. The supporting means may also be of spider-like ~; design. To fix the position of the individual discs in the tube or reaction chamher, it is possible to attach each supporting means to the wall of the tube or reaction chamber. Advantageously, I however, only the first and last supporting means are attached;
- the intermediate discs are, if located closely together, - automatically held in place transversely to the direction of flow. In a vertical tube or reaction chamber, only the bottom grid-like supporting means need be attached to the wall of the tube; the remaining discs and supporting means are then placed on to~p of the bottom disc.
` It has proved particularly advantageous to provide the ring-shaped bands with wall cut-outs (as in the case of conven-, :
tional packing rings) which project into the spaces between the individual ring-shaped bands and are generally arranged, as the bands themselves, parallel to the direction of flow. Depending on ~the width of the band, the wall cut-outs may be arranged in one row or more, e.g., 2 rows. As a rule, there are from 40 to 125 wall cut~outs per meter oE band. ~ beneficial effect on the flow of very viscous fluids is achieved if the wall cut-outs arranged at right angles to the direction of flow are three-dimensionally twisted in the manner of a plowshare. The twist is shaped like the beyinning of a left-hand or right-hand helix. The cut-outs .
can therefore be twisted in the manner of a plowshare, alternating ~A~ 5 -~"' ' .
3~Z
in the c;~ns~ of a le~t-hand ~eliY and a r:i.ght-harl(l heli~ from di~c to disc and from band to band. In a particwlarl~ a~vant~geous arrangernent, the wal.l cut~outs ln a firc;t disc are twi.st~d as in a lef-t-lland helix, whilst i.n the next disc the wall cut-outs are twisted as in a right-hand helix.
~; It is also possible for the wall cut-ou-ts in a firstdisc to point inwards, i.e., toward the axis oE the reaction chamber, and in a second disc ~viewed in the direc-tion of flow) . for them to point outwards, i.e., toward the wall of the tube or reaction chamber. It has also proved advantageous so to construct the wall cut-outs that they serve as spacers between the individual ring shaped bands.
Preferred embodiments of the invention will now be explained with reference to the appended drawings, wherein:
Fig. 1 shows a cross-section through a disc contained in an apparatus according to the invention;
:: ' : Fig. 2 shows a plan view of two mutually staggered ;; discs, of each o.f which only one half is shown; and -Fig. 3 which is on the same sheet as Fig. 1 shows an enlarged part section of Fig. 1.
In Fig. 1, the displacer body 1 with conical top and bottom ends is attached to.the supporting means 4 for ~xample by welding. The,supporting means 4 is for instance a wide~
~ meshed grid of sheet metal arranged parallel to the direction of; flow. The ring~shaped bands 2 are concentrically arranged around the displacer body 1 with increasing diameter, each band beingthe same distance from the next, and attached to the supporting means 4. The ring-shaped bands have wall cut-outs 3. For the sake of clarity/ only the wall cut-outs.of the last band before - 30 the reactor wall 5 are shownO The right-hand portlon of Fig. 1 ~:
(not shown) is of course completely symmetrical with the left-hand portion. The attachment of the suppor-ting means 4 to the reactor wall 5 is not shown in Fig. 1 either, because in the case of ~. ~
: ~" ~ : : ,, ' : . . : .
~: , . ,;.; :
3~ LZ
vertical tubes advclrltageowsl~ only the bottom supporting means is attached to the rcac~or wa1:1.
In Fig. 2, two discs A and s are arranyed one in front of -the other inslde the reactor wall 5. Discs ~ and B each consist of a displacer body 1, concentrically arranged ring-shaped bands 2 and wall cu-t-outs 3. For the sake of clarity, only the right-hand half of disc A and only the lef-t-hand half of disc B are shown. In disc A, -the wall cut-outs 3 poin-t inwards, i.e., toward the displacer body 1, whereas, in disc s, the wall cut-outs 3 point outwards, i.eO, toward the reactor wall 5.
The supporting means 4 has a spider-like shape and is shown as dashed lines. Again for the sake of clarity, only the supporting means for one disc is shown. The ring-shaped bands of disc A and those of disc B are of course attached to the same kind of supporting means 4. The attachment of the supporting means 4 ` to the reactor wall 5 is not shown either, as the manner in which it is attached is adapted to existing conditions.
' Fig. 3 shows a part section of Fig. 1, the ring-shaped `', band being attached to the grid-like supporting means 4. The ,1 . .
'~ 20 ~ring-shaped band has 2 rows of wall cut-outs 3 which are twisted.
.
Fig. 3 is limited on the left-hand side by the reactor wall 5.
For the sake of clarity, the attachment of the supporting means-
are o~ particul~r industrial impo~tance in connection ~Jith the manu~acture o~ polycaprolactam.
n accord~nce with the inverltion, the ver~ viscous li~uid ls passed through annular spaces. l'he width of the spaces is advantageously ~rom 1.75 to 5 cm. The spaces extend concentrically with increasing diame-ter over the entire cross-seetion o~ the tube or reaction cham~er. The term "concentrically" means that the distanee b~-tween any one annular space and -the axis of the tube or reaction ehamber is the same at all points, and the distanee between any one annular spaee and the walls of the tube or reaction chamber is the same at all points. The annular spaees - are formed by eoneentrieally arranged ring-shaped bands of inereasing diameter. The width of all the bands of any one dise is the same. The walls of the ring-shaped bands run parallel to the `~ direction of ~low of the very viscous liquid and eonsequently parallel to the walls of the tube or reaction chamber. In aeeordanee with the invention, the annular spaees have the same ; depth in the direetion of flow and run parallel, as viewed in the direetion of flow. As the very viseous liquid flows through the tube or reaetion chamber, it is passed -twiee or more times through annular spaces extending eoneentrically with inereasing diameter over the entire eross-section of the tube or reaetion chamber, the seeond and subsequent annular spaees being staggered with - respeet to the preeeding annular spaee. The depth of the annular spaees in the direetion of flow is advantageously from 1.5 to 10, espeeially 3.5 to 8, em. Once the depth has been seleeted, it remains the same for all the annular spaees of a dise over the entire cross-seetion of the tube or reaetion ehamber. As a rule, the width of the annular spaees, i.e., the distanee between the bands, is eonstant over the entire eross-seetion of the tube or reaetion ehamber. However, it is also possible for the width of the annular spaees to increase or deerease with inereasing diameter ~ 3 ~
.
1~3~
so as to counterbalarlc~ a chancJe in the flow charact~risticc.
of 'che melt, as may arisc, ~or inst:ance, through additional int~rnal or ex~ernal heatincJ.
The very viscous 1iquld flows at least twice~ through concentric annular spaces extending over the entire cross-section of the tube or reaction chamber. The annular spaces are advan-tageously from 3.5 to 20 cm apart, in -the direction of flow. It has proved to be particularly aclvantayeous to pass the highly viscous melt through annular spaces from 4 -to lO times per meter of reaction chamber.
The new apparatus comprises two or more discs arranged at axial intervals within a tube or reactlon chamber transversely to the direction of flow~ ~dvantageously, the dis-tance, in the direction of flow, between the discs is from 3.5 to 20 cm. It has ~-~ proved advantageous to use from 4 to 10 discs per meter length, in reaction chambers. In another advantageous embodiment, the discs are solely separated from one another by the support structure (described in more detail below) which serves as a spacer.
In a vertical reaction chamber, therefore, only the support , structure of the bottom disc is attached to the walls of the chamber, or simply placed on an annular bead in the wall of the ` tube or reaction chamber, and the remaining discs with their , support structures are placed on top.
~ Each disc consists of a plurality of ring-shaped bands ; of increasing diameter, the bands being arranged freely of one another and concentrically at intervals on a grid supporting means.
The ring-shaped bands are preferably from 1.5 to lO cm wide, and especially from 3.5 to 8 cm wide. The distance between the indi-vidual ring-shaped bands is advantageously from 1.75 to 5 cm. As a rule, the distances between the individual ring-shaped bands are constant. However, it is also possible to arrange the ring-shaped bands, of increasing diameter, at larger or smaller distances so .:
' . ~ , -~0~3~
as to counterbalance a challcJe in ~he flow characteristics of the melt, as may arisc, e.g., throucJh additional in~ernal or e~ternal heating. In order ~o prevent thc vi~cous eluid in the center oE
the disc from moving Easter, a displacer body is advantageou51y provided there, -the body preferably haviny conical ends.
To prevent the concentrically arranged bands from moving, they are attached, e.g., by welding, to a grid-like support. The support is for example a wide-meshed grid consistiny of profiles, or a sheet metal grid, the walls of which run parallel to the direction of flow. The supporting means may also be of spider-like ~; design. To fix the position of the individual discs in the tube or reaction chamher, it is possible to attach each supporting means to the wall of the tube or reaction chamber. Advantageously, I however, only the first and last supporting means are attached;
- the intermediate discs are, if located closely together, - automatically held in place transversely to the direction of flow. In a vertical tube or reaction chamber, only the bottom grid-like supporting means need be attached to the wall of the tube; the remaining discs and supporting means are then placed on to~p of the bottom disc.
` It has proved particularly advantageous to provide the ring-shaped bands with wall cut-outs (as in the case of conven-, :
tional packing rings) which project into the spaces between the individual ring-shaped bands and are generally arranged, as the bands themselves, parallel to the direction of flow. Depending on ~the width of the band, the wall cut-outs may be arranged in one row or more, e.g., 2 rows. As a rule, there are from 40 to 125 wall cut~outs per meter oE band. ~ beneficial effect on the flow of very viscous fluids is achieved if the wall cut-outs arranged at right angles to the direction of flow are three-dimensionally twisted in the manner of a plowshare. The twist is shaped like the beyinning of a left-hand or right-hand helix. The cut-outs .
can therefore be twisted in the manner of a plowshare, alternating ~A~ 5 -~"' ' .
3~Z
in the c;~ns~ of a le~t-hand ~eliY and a r:i.ght-harl(l heli~ from di~c to disc and from band to band. In a particwlarl~ a~vant~geous arrangernent, the wal.l cut~outs ln a firc;t disc are twi.st~d as in a lef-t-lland helix, whilst i.n the next disc the wall cut-outs are twisted as in a right-hand helix.
~; It is also possible for the wall cut-ou-ts in a firstdisc to point inwards, i.e., toward the axis oE the reaction chamber, and in a second disc ~viewed in the direc-tion of flow) . for them to point outwards, i.e., toward the wall of the tube or reaction chamber. It has also proved advantageous so to construct the wall cut-outs that they serve as spacers between the individual ring shaped bands.
Preferred embodiments of the invention will now be explained with reference to the appended drawings, wherein:
Fig. 1 shows a cross-section through a disc contained in an apparatus according to the invention;
:: ' : Fig. 2 shows a plan view of two mutually staggered ;; discs, of each o.f which only one half is shown; and -Fig. 3 which is on the same sheet as Fig. 1 shows an enlarged part section of Fig. 1.
In Fig. 1, the displacer body 1 with conical top and bottom ends is attached to.the supporting means 4 for ~xample by welding. The,supporting means 4 is for instance a wide~
~ meshed grid of sheet metal arranged parallel to the direction of; flow. The ring~shaped bands 2 are concentrically arranged around the displacer body 1 with increasing diameter, each band beingthe same distance from the next, and attached to the supporting means 4. The ring-shaped bands have wall cut-outs 3. For the sake of clarity/ only the wall cut-outs.of the last band before - 30 the reactor wall 5 are shownO The right-hand portlon of Fig. 1 ~:
(not shown) is of course completely symmetrical with the left-hand portion. The attachment of the suppor-ting means 4 to the reactor wall 5 is not shown in Fig. 1 either, because in the case of ~. ~
: ~" ~ : : ,, ' : . . : .
~: , . ,;.; :
3~ LZ
vertical tubes advclrltageowsl~ only the bottom supporting means is attached to the rcac~or wa1:1.
In Fig. 2, two discs A and s are arranyed one in front of -the other inslde the reactor wall 5. Discs ~ and B each consist of a displacer body 1, concentrically arranged ring-shaped bands 2 and wall cu-t-outs 3. For the sake of clarity, only the right-hand half of disc A and only the lef-t-hand half of disc B are shown. In disc A, -the wall cut-outs 3 poin-t inwards, i.e., toward the displacer body 1, whereas, in disc s, the wall cut-outs 3 point outwards, i.eO, toward the reactor wall 5.
The supporting means 4 has a spider-like shape and is shown as dashed lines. Again for the sake of clarity, only the supporting means for one disc is shown. The ring-shaped bands of disc A and those of disc B are of course attached to the same kind of supporting means 4. The attachment of the supporting means 4 ` to the reactor wall 5 is not shown either, as the manner in which it is attached is adapted to existing conditions.
' Fig. 3 shows a part section of Fig. 1, the ring-shaped `', band being attached to the grid-like supporting means 4. The ,1 . .
'~ 20 ~ring-shaped band has 2 rows of wall cut-outs 3 which are twisted.
.
Fig. 3 is limited on the left-hand side by the reactor wall 5.
For the sake of clarity, the attachment of the supporting means-
4 to the reactor wall 5 is not shown.
J' ~ ~
.
' .. , .. , , ~ ~ .
, '.' ' , . , ' ; .~: :' ,.
J' ~ ~
.
' .. , .. , , ~ ~ .
, '.' ' , . , ' ; .~: :' ,.
Claims (8)
1. A process for achieving a uniform flow profile of very viscous liquids when flowing through a tube or reaction chamber, wherein the very viscous liquid is passed through at least two sets of annular spaces arranged at axial intervals within the tube or reaction chamber, the annular spaces of each set extending concentrically with increasing diameter over the entire cross-section of the tube or reaction chamber and having the same depth in the direction of flow, the annular spaces of two consecutive sets being staggered with respect to each other as viewed in the direction of flow.
2. Apparatus for achieving a uniform flow profile of a very viscous fluid when flowing through a tube, comprising in combination two or more discs arranged at axial intervals within a flow tube transversely to the direction of flow, each disc consisting of a plurality of ring-shaped bands of increasing diameter, the bands being arranged freely of one another and concentrically at intervals on a grid supporting means of said tube to provide correspondingly concentric open spaces there-between over the entire cross-section of the tube, with the walls of the bands running parallel to the direction of flow and the bands of the separate discs being staggered with respect to each other as viewed in the direction of flow.
3. Apparatus as claimed in claim 2, wherein the ring-shaped bands are provided with wall cut-outs which project into the annular spaces between the individual ring-shaped bands and are arranged parallel to the direction of flow.
4. Apparatus as claimed in claim 2, wherein the ring-shaped bands are provided with wall cut-outs which project into the annular spaces between the individual ring-shaped bands and are arranged with a three-dimensional twist to the left or right of a parallel to the direction of flow.
5. Apparatus as claimed in claim 4, wherein the wall cut-outs alternate in the sense of a left-hand and a right-hand twist from band to adjacent band and from disc to adjacent disc.
6. Apparatus as claimed in claim 4, wherein the wall cut-outs project inwardly and outwardly alternately from disc to adjacent disc.
7. Apparatus as claimed in claim 2, wherein an axially elongated displacer body having conical ends is located on the supporting means in the center of each disc.
8. Apparatus as claimed in claim 4, wherein the wall cut-outs also act as spacers between the individual ring-shaped bands of each disc.
Applications Claiming Priority (2)
| Application Number | Priority Date | Filing Date | Title |
|---|---|---|---|
| DEP2514129.1 | 1975-03-29 | ||
| DE19752514129 DE2514129C3 (en) | 1975-03-29 | 1975-03-29 | Device for achieving a uniform flow profile |
Publications (1)
| Publication Number | Publication Date |
|---|---|
| CA1083012A true CA1083012A (en) | 1980-08-05 |
Family
ID=5942805
Family Applications (1)
| Application Number | Title | Priority Date | Filing Date |
|---|---|---|---|
| CA247,615A Expired CA1083012A (en) | 1975-03-29 | 1976-03-10 | Process and apparatus for achieving a uniform flow profile |
Country Status (10)
| Country | Link |
|---|---|
| JP (1) | JPS51117319A (en) |
| BE (1) | BE840167A (en) |
| CA (1) | CA1083012A (en) |
| CH (1) | CH606820A5 (en) |
| DE (1) | DE2514129C3 (en) |
| ES (1) | ES446430A1 (en) |
| FR (1) | FR2306356A1 (en) |
| GB (1) | GB1555804A (en) |
| IT (1) | IT1056965B (en) |
| NL (1) | NL174387C (en) |
Families Citing this family (9)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| DE3908401A1 (en) * | 1989-03-15 | 1990-09-20 | Ruhrgas Ag | Method and device for rectifying a disturbed flow |
| DE3921572C2 (en) * | 1989-06-30 | 1993-11-18 | Veba Kraftwerke Ruhr | Rectifier for installation in duct parts in front of flue gas cleaning systems |
| DE4025434A1 (en) * | 1990-08-10 | 1992-02-13 | Emitec Emissionstechnologie | HONEYCOMB BODY WITH CROSS-SECTIONAL AREAS OF DIFFERENT CHANNEL SIZES, IN PARTICULAR CATALYST SUPPORT BODY |
| DE4111606C1 (en) * | 1991-04-10 | 1992-08-06 | Axel Dipl.-Ing. 3340 Wolfenbuettel De Struck | Fluid flow distribution with flow obstacles - which deflect as diffusion two part-flows orthogonally to total flow direction |
| JPH0535815U (en) * | 1991-10-08 | 1993-05-14 | 株式会社橋千商会 | Handbag |
| FR2683003B1 (en) * | 1991-10-25 | 1995-02-17 | Schlumberger Ind Sa | FLOW RECTIFIER. |
| DE10020571A1 (en) * | 2000-04-27 | 2001-10-31 | Beiersdorf Ag | Apparatus evening-out flow of high viscosity fluids along closed lines includes vessel with self-regulating plate closure and outlet pump |
| DE10025061C1 (en) * | 2000-05-23 | 2002-05-02 | E On Kraftwerke Gmbh | Wash tower for flue gas desulfurization plants |
| CN110259772B (en) * | 2019-06-17 | 2020-05-26 | 杭州凯维阀门集团有限公司 | Water flow excitation type ball valve with paddle |
Family Cites Families (1)
| Publication number | Priority date | Publication date | Assignee | Title |
|---|---|---|---|---|
| GB1469648A (en) * | 1973-03-23 | 1977-04-06 | Tokico Ltd | Liquid flow straightening device |
-
1975
- 1975-03-29 DE DE19752514129 patent/DE2514129C3/en not_active Expired
-
1976
- 1976-03-08 JP JP2428776A patent/JPS51117319A/en active Pending
- 1976-03-09 IT IT2099676A patent/IT1056965B/en active
- 1976-03-10 CA CA247,615A patent/CA1083012A/en not_active Expired
- 1976-03-24 CH CH368376A patent/CH606820A5/xx not_active IP Right Cessation
- 1976-03-25 FR FR7608643A patent/FR2306356A1/en active Granted
- 1976-03-26 ES ES446430A patent/ES446430A1/en not_active Expired
- 1976-03-26 GB GB1220076A patent/GB1555804A/en not_active Expired
- 1976-03-26 NL NL7603222A patent/NL174387C/en not_active IP Right Cessation
- 1976-03-29 BE BE165671A patent/BE840167A/en not_active IP Right Cessation
Also Published As
| Publication number | Publication date |
|---|---|
| NL7603222A (en) | 1976-10-01 |
| FR2306356A1 (en) | 1976-10-29 |
| IT1056965B (en) | 1982-02-20 |
| ES446430A1 (en) | 1977-06-16 |
| CH606820A5 (en) | 1978-11-15 |
| DE2514129B2 (en) | 1978-06-29 |
| DE2514129C3 (en) | 1979-03-01 |
| FR2306356B1 (en) | 1980-01-25 |
| NL174387B (en) | 1984-01-02 |
| DE2514129A1 (en) | 1976-09-30 |
| JPS51117319A (en) | 1976-10-15 |
| NL174387C (en) | 1984-06-01 |
| BE840167A (en) | 1976-09-29 |
| GB1555804A (en) | 1979-11-14 |
Similar Documents
| Publication | Publication Date | Title |
|---|---|---|
| CA1083012A (en) | Process and apparatus for achieving a uniform flow profile | |
| US3941350A (en) | Quieting means for a fluid flow control device using vortical flow patterns | |
| US5437784A (en) | Injector for a flotation device | |
| EP0260736B1 (en) | A method of mixing two or more gas flows | |
| CA2980770C (en) | Modal attenuator | |
| GB2032610A (en) | Apparatus for a treatment of flowing media which causes heat exchange and mixing | |
| WO2004092687A1 (en) | Differential pressure means for a gas meter arrangement, comprising an improved flow geometry | |
| CN107847630A (en) | The reaction core system of light catalytic purifying agent | |
| Shuli | Hydrodynamic studies on heat exchangers with helical baffles | |
| JPH05200262A (en) | Stationary mixing member with deflection body and mixing device | |
| WO2008140867A9 (en) | Baffle for generating multiple helical vortices in a fluid stream | |
| US4136976A (en) | Static mixing device | |
| CA2162540A1 (en) | Reactor apparatus for preparing a polymeric material | |
| EP0738373A1 (en) | Stationary material mixing apparatus | |
| EP0580099A2 (en) | Ultrasonic gas meter | |
| RU2013132420A (en) | NEW FILTERING ELEMENT GEOMETRY | |
| DE102006060507A1 (en) | Reactor for carrying out a reaction between two fluid educts on a catalyst bed with premixing of the fluid educts in a mixing device | |
| EP0268005A2 (en) | Rotational oscillation damper | |
| RU97113521A (en) | METHOD AND DEVICE FOR CONTROLLED DISPERSION OF LIQUID JETS | |
| RU2012146440A (en) | REACTOR FOR GAS-LIQUID TWO-PHASE REACTIONS | |
| US10611654B2 (en) | Municipal mixing with reciprocating motion disk | |
| US4202375A (en) | Process and apparatus for achieving a uniform flow profile | |
| DE102014009527B4 (en) | Modifiable UV tube reactor | |
| EP0005535B1 (en) | Method and apparatus for exchange of mass and/or of heat by direct contact and for mixing of gaseous or vaporous and liquid or solid media | |
| DE102016106843A1 (en) | Fluid treatment device |
Legal Events
| Date | Code | Title | Description |
|---|---|---|---|
| MKEX | Expiry |